EP0111176B1 - Process and device for the instant production of reduced iron pellets and liquid iron from iron oxide pellets - Google Patents

Process and device for the instant production of reduced iron pellets and liquid iron from iron oxide pellets Download PDF

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Publication number
EP0111176B1
EP0111176B1 EP83111296A EP83111296A EP0111176B1 EP 0111176 B1 EP0111176 B1 EP 0111176B1 EP 83111296 A EP83111296 A EP 83111296A EP 83111296 A EP83111296 A EP 83111296A EP 0111176 B1 EP0111176 B1 EP 0111176B1
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EP
European Patent Office
Prior art keywords
gas
melt
process according
grain fraction
down gasifier
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP83111296A
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German (de)
French (fr)
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EP0111176A1 (en
Inventor
Bogdan Dipl.-Ing. Vuletic
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Voestalpine AG
Deutsche Voest Alpine Industrieanlagenbau GmbH
Original Assignee
Voestalpine AG
Deutsche Voest Alpine Industrieanlagenbau GmbH
Korf Engineering GmbH
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Application filed by Voestalpine AG, Deutsche Voest Alpine Industrieanlagenbau GmbH, Korf Engineering GmbH filed Critical Voestalpine AG
Priority to AT83111296T priority Critical patent/ATE19658T1/en
Publication of EP0111176A1 publication Critical patent/EP0111176A1/en
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Publication of EP0111176B1 publication Critical patent/EP0111176B1/en
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    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
    • C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
    • C21B13/002—Reduction of iron ores by passing through a heated column of carbon
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
    • C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
    • C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/42—Sulphur removal
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2

Definitions

  • the invention relates to a method according to the preamble of claim 1. Furthermore, it relates to a system according to the preamble of claims 25 and 32.
  • lumpy iron ore is to be understood to mean iron ore in any lumpy form, ie also in the form of pellets.
  • a method and a plant of this type are known from DE-C2-30 34 539.
  • the known method about 40% more reducing gas is produced when the sponge iron melts than is required to produce the same amount of sponge iron.
  • each coupling of several systems leads to a reduction in the availability of the overall system and thus to a deterioration in economy.
  • Small iron sponge particles stay longer in the fluidized bed, warm up to a higher temperature and are melted faster.
  • the object of the invention is to make available a method of the type mentioned in the introduction, which works economically without excess gas and with which the specific performance of the melter gasifier can be increased and its mode of operation can be improved. Furthermore, it is an object of this invention to make a system available for carrying out this method.
  • the method according to the invention is characterized by the features of claim 1. Advantageous embodiments of this method can be found in claims 2 to 24.
  • the system according to the invention is characterized by the features of claim 25.
  • Advantageous embodiments of the device according to the invention are described in claims 26 to 36.
  • the entire amount of the sponge iron particles produced in the direct reduction unit is not supplied to the melter gasifier, but only a part, so that less gas is produced when this partial amount is melted, and an excess of reducing gas can be avoided in this way.
  • the partial quantity of sponge iron particles supplied to the melter gasifier is selected insofar as the upper limit of the particle size is limited. This avoids that larger pieces of iron sponge migrate through the coal fluidized bed without sufficient heating and then there is a build-up of material which can only be melted with increased energy expenditure in the melting zone of the melter gasifier.
  • the coarse grain fraction separated on the way from the reduction unit to the melter gasifier can either be fed to another meltdown vessel, such as an electric arc furnace, when hot, but it can also be hot-briquetted, passivated or cooled in order to be available as a feedstock for a melter.
  • another meltdown vessel such as an electric arc furnace
  • part of the blast furnace gas of the direct reduction unit as an oxygen carrier to the melter gasifier and to gasify part of the coal by endothermic reactions with the carbon dioxide and the water vapor in the blast furnace gas.
  • the coarse grain separator must be designed for temperatures between 700 ° and 900 ° C, since the sponge iron particles leave the direct reduction unit with these temperatures. With some classifiers, especially when using screens, this can cause difficulties.
  • the separated sponge iron particles are preferably cooled by cooled, cleaned and treated top gas from the reduction unit, which after the heat exchange with the sponge iron particles is admixed to the hot reducing gas stream directed from the melting gasifier to the reducing unit for temperature control. In this way, the top gas of the reduction unit is also used economically.
  • the separation of the sponge iron particles of the coarse grain fraction increases the relative proportion of fine material of the sponge iron fed to the melter and thus also the amount of possible discharge of fine material from the melter.
  • the point at which the sponge iron particles are released within the melter gasifier is therefore moved down from the lid of the vessel to the vicinity of the upper limit of the coal fluidized bed. This is preferably done through a downpipe which dips from above into the interior of the melter gasifier up to the vicinity of the upper limit of the coal fluidized bed formed in the melter gasifier.
  • the sponge iron particles For a metered supply of the sponge iron particles into the melter gasifier, it is expedient to provide a discharge device between the coarse grain separator and the melter gasifier, through which the downpipe or the downpipes are supplied in a controlled amount with sponge iron particles.
  • the flow resistance for the reducing gas rising via the downpipe can also be increased and overheating and sintering of the sponge iron particles in the area of the coarse grain separator and in the lower part of the reduction unit can be avoided.
  • the plant shown schematically in Fig. 1 for the direct production of molten pig iron from lumpy iron ore contains a melter gasifier 1 of the type described in EP-B1-0010627. Above the melter gasifier, a shaft furnace 2 is arranged, which according to its mode of operation with the upper part of a Blast furnace or a direct reduction shaft furnace can be compared. The latter is described in principle, for example, in DE-A-29 35 707. Pieces of iron ore are fed to the direct reduction shaft furnace from above - indicated by an arrow 3 - which sinks in the shaft furnace in the form of a loose bed and is reduced to sponge iron by means of a hot reducing gas at a temperature of about 750 ° and 900 ° C. which is blown in via a central gas inlet 4 .
  • the used reducing gas hereinafter called blast furnace gas, leaves the shaft furnace 2 via an upper gas outlet 5.
  • the hot sponge iron produced by reduction of the lumpy iron ore is discharged from the direct reduction shaft furnace 2 at a temperature of approximately 750 ° to 850 ° C. and passes through a pipe 6 into a coarse grain separator 7.
  • a thermally resilient sieve with a mesh size of z. B. 12 mm, are retained by the sponge iron particles with a size of more than 12 mm.
  • the sponge iron particles of the fine grain fraction leave the coarse grain separator 7 via a first outlet opening 8 and pass through a pipe 9 into a discharge device 10 which contains, for example, a scraper or a screw.
  • the sponge iron particles of the coarse grain fraction leave the coarse grain separator 7 through a second outlet opening 11 and reach a cooling unit 13 via a pipe 12, in which they are cooled down to room temperature, so that they can be transported to the point at which they are processed without great risk of reoxidation should be.
  • the exit of the cooled sponge iron particles from the cooling unit 13 is denoted by 14.
  • the discharge device 10 has at the lower end an outlet opening 16 for the sponge iron particles, which at least one down pipe 17 is connected to the interior of the melter gasifier 1.
  • the sponge iron particles are dispensed in a metered manner via the outlet opening 16.
  • the feed materials required for the melter gasifier are added continuously or intermittently in the amount required for the melter process via the downpipe 17.
  • the amount of coal required to form and maintain the coal fluidized bed is added directly to the melter gasifier via a pipe 15.
  • the melter gasifier can be divided into three sections in the operating state, namely into a lower section 18, in which pig iron and slag are located, into a middle section 19 for the coal fluidized bed and into an extended section upper section 20, which serves as a relaxation room.
  • the sponge iron particles are not supplied at the upper limit of the calming space, but within the calming space near the upper limit of the coal fluidized bed 19. In the present case, this is done by immersing the downpipe 17 deeply into the calming space 20.
  • the amount of fine grain discharged with the gas from the melter gasifier which plays a special role in the process according to the invention in relation to the total amount of sponge iron brought into the melter gasifier, can be greatly reduced.
  • the cheapest immersion depth of the downpipe 17 can be easily determined experimentally.
  • the downpipe expediently ends just above the upper limit of the coal fluidized bed.
  • one or more downpipes 17 also makes it possible, either by deflecting these pipes at the lower end or by attaching baffle plates, to significantly reduce the vertical speed component of the falling material and thus to increase the residence time of the sponge iron particles in the coal fluidized bed. Because of the high thermal stress of a down pipe immersed in the interior of the melter gasifier, it is advisable to cool the pipe. One way of forming such a down pipe is described with reference to FIG. 2.
  • the channels 21 and 22 for tapping the pig iron and the slag and a nozzle 23 for blowing in an oxygen-containing gas are also indicated schematically in the melter gasifier 1.
  • the reducing gas generated in the melter gasifier 1 leaves the melter gasifier via the outlet 24 at a temperature of approximately 1200.degree. From here it is forwarded via the reducing gas line 25 to the gas inlet 4 of the direct reduction unit 2. Since the reducing gas introduced into the direct reduction unit 2 must not exceed a temperature of 900 ° C., the hot reducing gas stream rising in the line 25 for temperature control is mixed in at the point 26 with cooling gas which is supplied via the line 17. This cooling gas is recirculated top gas of the direct reduction unit 2, after it has been washed in a top gas scrubber 28 and cooled in a CO 2 absorption tower 29 of the CO 2 content has been reduced.
  • the blast furnace gas prepared in this way could already be mixed with the hot reducing gas from the melter gasifier for temperature control, in the exemplary embodiment described it was passed over the cooler 13 and, in the direct heat exchange with the iron sponge particles of the coarse grain fraction, causes these iron sponge particles to cool down.
  • the processed top gas heats up to approx. 500 ° C. It is then mixed via line 27 at point 26 into the hot reducing gas stream of line 25 in order to lower its temperature to a value below 900 ° C. If more iron sponge than pig iron is to be produced in the system, it is necessary to preheat a portion of the processed blast furnace gas in the separate recuperator 31 in parallel with the cooling unit 13 in order to be able to set the desired bus gas temperature.
  • the unprocessed top gas behind the top gas scrubber 28, the amount of which depends on the heat requirement, is to be used as the heating gas. This also prevents the circulation gas from being enriched with inactive components such as N 2 .
  • 30 denotes a compressor upstream of the CO 2 absorption tower 29, which generates the required pressure.
  • it is necessary to desulfurize the gas from the melter gasifier 1 in the hot gas desulfurization unit 32.
  • some cold gas can be added to this gas to adjust its temperature to the desulfurization process.
  • Fig. The part of a down pipe 17 immersed in the melter gasifier is shown in section. Because of the high thermal stress inside the melter gasifier, the downpipe has a liquid cooling system Mistake.
  • a liquid channel is formed by three metal tubes 31, 32 and 33 arranged concentrically to one another, through which a cooling liquid, for example water, is passed.
  • the cooling system is covered on all sides with a refractory layer 34.
  • the downpipe 17 shown contains measures by deflection to reduce the vertical speed of the falling sponge iron particles and thus to increase the dwell time here because of the reduced entry speed into the coal fluidized bed.
  • cascade-shaped projections 35 are provided in the lower region of the downpipe, on which material can deposit, which thereby serves as wear protection.
  • a baffle plate 36 preferably in the form of a blunt cone similar to a Chinese hat, can also be provided at the lower outlet opening of the tube.
  • the falling sponge iron particles are deflected and braked in a meandering manner by the projections 35 in the tube and deflected approximately in a horizontal direction by the baffle plate 36, as a result of which their vertical speed component is considerably reduced.
  • the ceiling of the melter gasifier is designated by 37 in FIG. 2.
  • the coarse-grain separator 7 shown schematically in FIG. 3 is designed in the form of an inclined gutter 38 with at least one connecting piece 39 branching off from it.
  • the pipe through which the sponge iron particles discharged from the direct reduction shaft furnace are fed is designated by 6
  • the first outlet opening for the fine-grain fraction is 8
  • the second outlet opening for the coarse-grain fraction is 11.
  • the bulk material entering the coarse grain separator 7 from above is naturally separated during the movement by the coarse grain separator, i. H. the fine particles settle down and the coarse particles collect on the top.
  • the flow profile shown schematically in FIG. H. the coarse iron sponge particles are essentially passed on via the downpipe 38 to the second outlet opening 12 and drawn off from there. 1 is controlled by a discharge device 10, which is connected via a tube to the coarse grain separator 7, then, as desired, the flow resistance for the gas rising from the melter gas can be kept relatively high.
  • a direct reduction shaft unit designed as a direct reduction shaft furnace 2 has an inlet device 3 for the lumpy iron ore and a gas outlet 5 for the used reducing gas (top gas) and a controllable discharge device 41 for the iron sponge particles obtained by direct reduction from the iron ore and a gas inlet 4 for hot reducing gas.
  • the melter gasifier 1 essentially corresponds to the melter gasifier of the first embodiment.
  • the ceiling of the upper section 20 serving as a calming space here has a chamber called a carburetor head 42, which is in communication with the calming space.
  • a gas outlet 43 for the reducing gas (raw gas) generated in the melter gasifier is provided in the gasifier head.
  • a gas inlet 44 for scrubbed and treated top gas from the direct reduction shaft furnace is provided in the gasifier head.
  • the pipe 15 for the addition of coal and the immersion pipe 17 for the addition of the fine grain fraction are also carried out through the ceiling of the melter gasifier.
  • Outlets 21 for liquid pig iron and 22 for liquid slag are provided in the lower region of the melting gasifier, furthermore at least one nozzle 23 or at least one burner 23a is provided above the slag level for blowing in gases and fine-grained solids.
  • the cooling unit 13a for the hot sponge iron particles discharged by the discharge device 41 there is a cooling unit 13a for the hot sponge iron particles discharged by the discharge device 41.
  • the inlet opening 46 of the cooling unit 13a for the hot sponge iron particles is connected to the discharge device 41 through the downpipe 6.
  • the down pipe 6 is assigned a level measuring device 47, by means of which the discharge device 41 can be controlled.
  • the cooling unit 13a has an outlet 48 for the cooling gas in the upper region next to the inlet opening 46 for the hot sponge iron particles and an inlet 49 for the cooling gas in the lower region next to an outlet opening 14 for the cooled sponge iron particles.
  • cooling takes place in countercurrent and in direct exchange with the iron sponge particles sinking in the cooling unit. Since not only the coarse grain fraction of the iron sponge particles is fed to the cooling unit 13a, as in the embodiment according to FIG. 1, it is expedient to provide the cooling unit in the upper region with a calming space in order to keep the discharge of fine particles as low as possible. This can be done, for example, by inserting the downpipe 6 into the cooling unit in a certain length, so that a calming space is formed above the pouring cone within the cooling unit.
  • a classifying device 7a designed as a sieving station, by means of which the sponge iron particles are separated into a fine-grain fraction and a coarse-grain fraction.
  • the outlet opening 8 for the fine-grain fraction is connected by the pipeline 9 to the fine-grain container 10 arranged above the melter gasifier, the outlet opening 16 of which is connected to the dip tube 17.
  • the classifying device 7a is not arranged above the melter gasifier 1 due to lack of space and the pipeline 9 cannot be designed as a downpipe, suitable conveying means for the fine-grain fraction must be provided in this pipeline. If the separation takes place in the classifying device 7a in such a way that the fine-grain fraction contains only parts with a grain size of up to 3 mm, then it may be expedient to blow at least part of this fraction into the melter gasifier via the nozzles 23 and 23a. Appropriate pipelines to the nozzles must then be provided.
  • a pipe 12 is connected to the outlet opening 11 of the classifying device 7a for the coarse grain fraction, which is excreted from the process, through which the coarse grain fraction can be fed to a separate melting unit or a device for compacting, passivating or also a further cooling unit 13 according to FIG. 1 , to which the processed blast furnace gas is fed as a cooling medium.
  • a top gas scrubber 28 is connected to the top gas outlet 5 of the direct reduction shaft furnace, and the gas outlet 51 of the top gas scrubber 28 is connected via pipes 52 and 53 to a CO 2 absorption tower 29, whose gas outlet 54 is connected via lines 55 and 56 is connected to the inlet 49 of the cooling unit 13a for the cooling gas.
  • a pipeline 27 is provided from the gas outlet 48 of the cooling unit 13a to the reducing gas line 25 in order to admix the blast furnace gas which has been processed and heated in the cooling unit 13a with the reducing gas stream which is conducted via this line to the gas inlet 4 of the direct reduction shaft furnace 2.
  • the cooling unit 13a is assigned a cooling gas circuit 57 containing the pipeline 56 with a cooling gas scrubber 58 and a compressor 30a. This takes into account the fact that a larger amount of cooling gas is required for cooling in the cooling unit than processed top gas supplied via the pipeline 55 is available.
  • a pipeline 59 branches off to the inlet 44 in the carburetor head 42, into which a connecting line 60 to the gas outlet 54 of the CO 2 absorption tower 29 opens.
  • Treated top gas of different temperatures can be supplied to the gasifier head 42 via the pipeline 59, so that the temperature can be set here to an optimum temperature for the hot gas desulfurization.
  • the outlet 43 in the gasifier head 42 for the reducing gas generated in the melter gasifier 1 is connected via a pipeline 61 to a cyclone 62, to the gas outlet 63 of which the reducing gas line 25 leading to the direct reduction unit is connected.
  • a pipeline 61 to a cyclone 62
  • the outlet opening 64 for the separated solids is connected by a pipeline 65 to a pipeline 66 which is connected via a compressor 30 to the gas outlet 51 of the top gas scrubber 28.
  • the pipeline 66 feeds part of the top gas leaving the top gas scrubber 28 to the burner 23a as an oxygen-containing gas, this gas also serving as a carrier gas for the separated solids of the cyclone 62.
  • Oxygen can also be supplied to the burner 23a or the nozzles 23 via a pipeline 67.
  • a branch line 68 leads from the pipeline 52 connected to the gas outlet 51 of the top gas scrubber 28 to a steam generator 69.
  • a part of the untreated top gas can thus be used as heating gas for the generation of steam which is required in the CO 2 absorption tower 29.
  • the requirement is also taken into account in a particularly economical manner, the sulfur content of the pig iron melted in the melter gasifier and that removed from the process To keep the coarse grain fraction of the iron sponge particles low if coal with a high sulfur content is used as an energy source.
  • measures are provided to reduce the amount of energy required for melting the fine grain fraction in the melter gasifier and the blast furnace gas of the direct reduction unit partly in the unprocessed state, partly after a C0 2 7 wash and after direct heat exchange in the cooling unit for the iron sponge particles discharged from the direct reduction unit Process.
  • the proportion of energy required by the combustion of coal for the heat of fusion is reduced in that, when the sponge iron particles are separated in the classifying device 7a, the proportion of the free-grain fraction is reduced compared to the coarse-grain fraction, i. H. the grain band of the fine-grain fraction fed to the melter gasifier 1 is reduced to particles up to a size of 5 mm, preferably 3 mm. Because of the longer dwell time in the fluidized bed of the melter gasifier, these particles can be consumed with a significantly lower energy expenditure, i. H. so melt with less coal and therefore less sulfur. It is then also possible to use a portion of the unprocessed top gas supplied by the top gas scrubber 28, which contains carbon dioxide and water vapor, for gasifying the coal.
  • part of the blast furnace gas is fed via line 66 to one or more burners 23a of the melter gasifier 1, which open into the coal fluidized bed.
  • the blast furnace gas as the carrier gas
  • the discharge of the cyclone 62 namely carbon particles and desulphurizing agent separated from the reducing gas, is also returned to the melter gasifier.
  • oxygen or air is fed to the burner via line 67 as a combustion medium and part of the blast furnace gas or the blast furnace gas / dust mixture is burned.
  • the amount of blast furnace gas supplied via the pipeline 66 should be set so that the carburetor head temperature in connection with other temperature control measures is between 850 ° and 1 250 ° C, preferably at 1 100 ° C.
  • the possible use of blast furnace gas as an oxygen carrier for carrying out the gasification can of course also reduce the oxygen consumption per ton of product and thus increase the economics of the process.
  • a further saving in coal and thus a further reduction in the sulfur content in the reducing gas and in the sponge iron can be achieved in that blast furnace gas processed in the CO 2 absorption tower is mixed with the reducing gas. 4 in that part of the blast furnace gas processed in the CO 2 absorption tower 29 is passed via the pipes 55 and 56 through the cooling unit 13a, this part heats up in direct contact with the hot sponge iron particles and then again a part thereof is fed to the reducing gas line 25 and a further part to the carburetor head 42 via the pipeline 59. The other part of the processed top gas supplied by the C0 2 7 absorption tower is fed directly to the gasifier head 42 via the pipe 60 and part of the pipe 59.
  • the amount of processed blast furnace gas mixed with the reducing gas can reduce the consumption of coal and oxygen, and thus the amount of sulfur introduced with coal, and the sulfur content in the reducing gas to about half.
  • a temperature control is also carried out with the processed blast furnace gas supplied to the gasifier head 42 via the pipe 59, the temperature in the pipe 59 being able to be determined by the proportion of the quantities supplied via the pipe 27 and the pipe 60.
  • the temperature setting in the carburetor head is particularly important when a desulfurizing agent is supplied to this or the exhaust line 61; to further reduce the sulfur content in the reducing gas.
  • the optimal temperature for hot gas desulfurization is approx. 900 ° C.
  • a desulfurizing agent such as hydrated lime, is fed to the gasification head 42 through the opening 45 in fine-grained form, and the optimum temperature for the hot gas desulfurization is set by the processed blast furnace gas blown through the gas inlet 44.
  • the desulphurization of the reducing gas takes place essentially in the gasifier head and in the exhaust line 61. Used and not yet used desulfurization agent is separated out in the cyclone 62 and returned to the melter gasifier via line 65.
  • the measures mentioned allow the sulfur content of the iron sponge particles to be reduced so much even when using sulfur-rich coal that the coarse-grain fraction which has been separated out can be processed in a steel mill without further measures for sulfur removal.
  • the fine grain fraction which for the reasons mentioned has a significantly higher sulfur content than the coarse grain fraction - due to the larger surface in relation to the weight, a larger amount of sulfur is bound by the fine sponge iron particles - is desulfurized and bound at least in part by the desulfurization agent supplied to the melter gasifier the desulfurizing agent is excreted through the slag.

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Abstract

In a process for the direct production of sponge iron particles and liquid crude iron from iron ore in lump form, which is reduced in a direct reduction unit and fed in a hot condition to a melting gasifier, the sponge iron particles which are discharged from the direct reduction unit are separated into a fine grain fraction and a coarse grain fraction, and only the fine grain fraction is fed to the melting gasifier. That ensures economy of operation, without an excess of gas.

Description

Die Erfindung betrifft ein Verfahren gemäß dem Gattungsbegriff des Patentanspruchs 1. Ferner bezieht sie sich auf eine Anlage gemäß dem Gattungsbegriff der Patentansprüche 25 und 32. Unter dem Begriff stückiges Eisenerz soll Eisenerz in beliebiger stückiger Form, also auch in Form von Pellets verstanden werden.The invention relates to a method according to the preamble of claim 1. Furthermore, it relates to a system according to the preamble of claims 25 and 32. The term lumpy iron ore is to be understood to mean iron ore in any lumpy form, ie also in the form of pellets.

Ein Verfahren und eine Anlage dieser Art sind durch die DE-C2-30 34 539 bekannt geworden. Bei dem bekannten Verfahren entsteht beim Einschmelzen des Eisenschwamms ca. 40 % mehr Reduktionsgas, als für die Erzeugung der gleichen Eisenschwamm-Menge erforderlich ist. Für einen wirtschaftlichen Betrieb der Anlage ist es erforderlich, daß Abnehmer für das überschüssige Gas vorhanden sind. Dies hat zur Folge, daß eine Koppelung mit anderen Anlagen erfolgen muß. Jede Koppelung von mehreren Anlagen führt jedoch zu einer Verringerung der Verfügbarkeit der Gesamtanlage und damit zu einer Verschlechterung der Wirtschaftlichkeit.A method and a plant of this type are known from DE-C2-30 34 539. In the known method, about 40% more reducing gas is produced when the sponge iron melts than is required to produce the same amount of sponge iron. For the plant to operate economically, it is necessary to have customers for the excess gas. As a result, it must be coupled to other systems. However, each coupling of several systems leads to a reduction in the availability of the overall system and thus to a deterioration in economy.

Je nach verwendetem Eisenerz werden aus dem Reduktionsaggregat auch größere Eisenschwammstücke ausgetragen, die das Kohlefließbett im Einschmelzvergaser schnell durchwandern, da sie schon mit großer Geschwindigkeit in den Beruhigungsraum eintreten, in dem sich ihre Fallgeschwindigkeit weiter erhöht. Aufgrund der kurzen Verweilzeit im Kohlefließbett ist ihre Erwärmung entsprechend geringer.Depending on the iron ore used, larger pieces of iron sponge are discharged from the reduction unit, which quickly move through the coal fluidized bed in the melter gasifier, since they enter the calming chamber at high speed, in which their falling speed increases further. Due to the short dwell time in the coal fluidized bed, their heating is correspondingly less.

Kleine Eisenschwammpartikel verweilen dagegen im Fließbett länger, erwärmen sich auf eine höhere Temperatur und werden schneller aufgeschmolzen.Small iron sponge particles, on the other hand, stay longer in the fluidized bed, warm up to a higher temperature and are melted faster.

Aufgabe der Erfindung ist es, ein Verfahren der einleitend genannten Art verfügbar zu machen, das ohne Gasüberschuß wirtschaftlich arbeitet und mit dem die spezifische Leistung des Einschmelzvergasers erhöht und dessen Arbeitsweise verbessert werden kann. Ferner ist es Aufgabe dieser Erfindung, eine Anlage zur Durchführung dieses Verfahrens verfügbar zu machen.The object of the invention is to make available a method of the type mentioned in the introduction, which works economically without excess gas and with which the specific performance of the melter gasifier can be increased and its mode of operation can be improved. Furthermore, it is an object of this invention to make a system available for carrying out this method.

Das erfindungsgemäße Verfahren ist durch die Merkmale des Anspruchs 1 gekennzeichnet. Vorteilhafte Ausgestaltungen dieses Verfahrens sind den Ansprüchen 2 bis 24 zu entnehmen. Die erfindungsgemäße Anlage ist durch die Merkmale des Anspruchs 25 gekennzeichnet. Vorteilhafte Ausgestaltungen der erfindungsgemäßen Vorrichtung sind in den Ansprüchen 26 bis 36 beschrieben.The method according to the invention is characterized by the features of claim 1. Advantageous embodiments of this method can be found in claims 2 to 24. The system according to the invention is characterized by the features of claim 25. Advantageous embodiments of the device according to the invention are described in claims 26 to 36.

Beim erfindungsgemäßen Verfahren wird dem Einschmelzvergaser nicht die gesamte Menge der im Direktreduktionsaggregat erzeugten Eisenschwammpartikel zugeführt, sondern nur ein Teil, so daß beim Einschmelzen dieser Teilmenge auch weniger Gas anfällt und auf diese Weise ein Überschuß an Reduktionsgas vermieden werden kann. Die dem Einschmelzvergaser zugeführte Teilmenge an Eisenschwammpartikeln ist insoferne ausgewählt, als die Partikelgröße nach oben begrenzt ist. Hierdurch wird vermieden, daß größere Eisenschwammstücke ohne ausreichende Erwärmung das Kohlefließbett durchwandern und es dann in der Schmelzzone des Einschmelzvergasers zu einer Anhäufung von nur mit erhöhtem Energieaufwand aufschmelzbarem Material kommt. Die auf dem Weg vom Reduktionsaggregat zum Einschmelzvergaser ausgeschiedene Grobkornfraktion kann entweder im heißen Zustand einem weiteren Einschmelzgefäß, wie einem Lichtbogenofen, zugeführt werden, sie kann aber auch heißbrikettiert, passiviert oder gekühlt werden, um als Einsatzmaterial für einen Schmelzofen zur Verfügung zu stehen.In the process according to the invention, the entire amount of the sponge iron particles produced in the direct reduction unit is not supplied to the melter gasifier, but only a part, so that less gas is produced when this partial amount is melted, and an excess of reducing gas can be avoided in this way. The partial quantity of sponge iron particles supplied to the melter gasifier is selected insofar as the upper limit of the particle size is limited. This avoids that larger pieces of iron sponge migrate through the coal fluidized bed without sufficient heating and then there is a build-up of material which can only be melted with increased energy expenditure in the melting zone of the melter gasifier. The coarse grain fraction separated on the way from the reduction unit to the melter gasifier can either be fed to another meltdown vessel, such as an electric arc furnace, when hot, but it can also be hot-briquetted, passivated or cooled in order to be available as a feedstock for a melter.

Da bei dem erfindungsgemäßen Verfahren nur die Feinkornfraktion im Einschmelzvergaser eingeschmolzen wird, können Schwierigkeiten entstehen, falls im Einschmelzvergaser unveredelte, schwefelreiche Kohle eingesetzt wird. Die Feinkornfraktion bindet nämlich wegen der auf das Gewicht bezogenen größeren Oberfläche der feinen Eisenschwammpartikel einen größeren Anteil des im Reduktionsgas enthaltenen Schwefels als die Grobkornfraktion, so daß es bei dem im Einschmelzvergaser erzeugten flüssigen Roheisen zu einem unerwünscht hohen Anstieg des Schwefelgehalts kommt. Es sind dann zusätzliche Maßnahmen zur Verringerung des Schwefelgehaltes erforderlich, die integriert in das erfindungsgemäße Verfahren einzeln oder in Kombination in den folgenden Schritten bestehen können :

  • 1. Dem Einschmelzvergaser wird ein Entschwefelungsmittel zugeführt.
  • 2. Der Anteil des durch Vergasung von Kohle erzeugten Rohgases im Reduktionsgas wird durch Beimischen eines Teils des Gichtgases des Direktreduktionsaggregates nach einer C02-Wäsche verringert; und
  • 3. der Anteil der Feinkornfraktion, die im Einschmelzvergaser eingeschmolzen wird, wird zur Einsparung an erforderlicher Schmelzwärme, die wiederum durch Verbrennung von Kohle aufgebracht werden muß, verringert.
Since only the fine-grain fraction is melted in the melter gasifier in the method according to the invention, difficulties can arise if unrefined, sulfur-rich coal is used in the melter gasifier. Because of the larger surface area of the fine iron sponge particles by weight, the fine grain fraction binds a larger proportion of the sulfur contained in the reducing gas than the coarse grain fraction, so that there is an undesirably high increase in the sulfur content in the molten pig iron produced in the melter gasifier. Additional measures for reducing the sulfur content are then required, which can be integrated into the process according to the invention individually or in combination in the following steps:
  • 1. A desulfurizing agent is fed to the melter gasifier.
  • 2. The proportion of the raw gas generated by gasification of coal in the reducing gas is reduced by admixing part of the blast furnace gas of the direct reduction unit after a CO 2 wash; and
  • 3. The proportion of the fine grain fraction which is melted down in the melter gasifier is reduced in order to save the required heat of fusion, which in turn has to be applied by burning coal.

.Bei der unter 3. genannten Maßnahme ist es auch möglich, dem Einschmelzvergaser einen Teil des Gichtgases des Direktreduktionsaggregates als Sauerstoffträger zuzuführen und durch endotherme Reaktionen mit dem Kohlendioxid und dem Wasserdampf im Gichtgas einen Teil der Kohle zu vergasen.With the measure mentioned under 3, it is also possible to supply part of the blast furnace gas of the direct reduction unit as an oxygen carrier to the melter gasifier and to gasify part of the coal by endothermic reactions with the carbon dioxide and the water vapor in the blast furnace gas.

Durch die Herabsetzung des Schwefelgehalts der Eisenschwammpartikel der Feinkornfraktion wird bei den genannten Maßnahmen auch eine wesentliche Herabsetzung des Schwefelgehaltes der Eisenschwammpartikel der Grobkornfraktion, die anderweitig verwertet werden, erreicht, so daß beim Einschmelzen dieser Eisenschwammpartikel keine besonderen Maßnahmen zur Schwefelentfernung mehr vorgesehen werden müssen.By reducing the sulfur content of the sponge iron particles of the fine-grain fraction, a significant reduction in the sulfur content of the sponge iron particles of the coarse-grain fraction, which are otherwise used, is achieved with the measures mentioned, so that no special sulfur removal measures need to be provided when these sponge iron particles are melted down.

Wird die Trennung der Eisenschwammpartikel in eine Feinkorn- und in eine Grobkornfraktion unmittelbar nach dem Austrag aus dem Direktreduktionsaggregat vorgenommen, dann muß der Grobkornabscheider für Temperaturen zwischen 700° und 900 °C ausgelegt sein, da die Eisenschwammpartikel das Direktreduktionsaggregat mit diesen Temperaturen verlassen. Bei einigen Klassiervorrichtungen, insbesondere bei der Verwendung von Sieben, kann dies zu Schwierigkeiten führen. In diesem Fall ist es zweckmäßig, die Klassierung der Eisenschwammpartikel erst nach einer Abkühlung vorzunehmen, wobei vorzugsweise gewaschenes und aufbereitetes Gichtgas des Direktreduktionsaggregates als Kühlmedium verwendet wird. In diesem Fall ist es zweckmäßig, Maßnahmen vorzusehen, durch die dem Kühlmedium der Weg über die Förderleitung der Eisenschwammpartikel in das Direktreduktionsaggregat versperrt bleibt.Will the separation of the sponge iron particles into a fine grain and a coarse grain fraction immediately after discharge from the direct reduction unit, then the coarse grain separator must be designed for temperatures between 700 ° and 900 ° C, since the sponge iron particles leave the direct reduction unit with these temperatures. With some classifiers, especially when using screens, this can cause difficulties. In this case, it is expedient to carry out the classification of the sponge iron particles only after cooling, preferably using washed and processed top gas from the direct reduction unit as the cooling medium. In this case, it is expedient to provide measures by which the path of the cooling medium via the delivery line of the sponge iron particles into the direct reduction unit remains blocked.

Eine Kühlung der ausgeschiedenen Eisenschwammpartikel erfolgt vorzugsweise durch abgekühltes, gereinigtes und aufbereitetes Gichtgas aus dem Reduktionsaggregat, das nach dem Wärmetausch mit den Eisenschwammpartikeln dem vom Einschmelzvergaser zum Reduktionsaggregat geleiteten heißen Reduktionsgasstrom zur Temperatursteuerung beigemischt wird. Auf diese Weise wird auch das Gichtgas des Reduktionsaggregates wirtschaftlich ausgenutzt.The separated sponge iron particles are preferably cooled by cooled, cleaned and treated top gas from the reduction unit, which after the heat exchange with the sponge iron particles is admixed to the hot reducing gas stream directed from the melting gasifier to the reducing unit for temperature control. In this way, the top gas of the reduction unit is also used economically.

Durch die Ausscheidung der Eisenschwammpartikel der Grobkornfraktion wird der relative Anteil an Feinmaterial des dem Einschmelzvergaser zugeführten Eisenschwammes erhöht und damit auch die Menge eines möglichen Austrags an Feinmaterial aus dem Einschmelzvergaser. Gemäß einer Weiterbildung der Erfindung wird deshalb die Stelle, an der die Eisenschwammpartikel innerhalb des Einschmelzvergasers freigegeben werden, vom Deckel des Gefäßes nach unten in die Nähe der Obergrenze des Kohlefließbettes verlegt. Dies geschieht vorzugsweise durch ein Fallrohr, das von oben in den Innenraum des Einschmelzvergasers bis in die Nähe der Obergrenze des sich in dem Einschmelzvergaser ausbildenden Kohlefließbettes eintaucht. Auf diese Weise ist es auch möglich, die Eisenschwammpartikel mit abgebremster Vertikalgeschwindigkeitskomponente zuzuführen, sei es durch eine entsprechende Umlenkung mittels kaskadenförmig angeordneter Vorsprünge im unteren Bereich des Fallrohres oder durch wenigstens ein Prallblech unterhalb des Fallrohres, das vorzugsweise in Form eines stumpfen Kegels ähnlich einem Chinesenhut ausgebildet ist.The separation of the sponge iron particles of the coarse grain fraction increases the relative proportion of fine material of the sponge iron fed to the melter and thus also the amount of possible discharge of fine material from the melter. According to a further development of the invention, the point at which the sponge iron particles are released within the melter gasifier is therefore moved down from the lid of the vessel to the vicinity of the upper limit of the coal fluidized bed. This is preferably done through a downpipe which dips from above into the interior of the melter gasifier up to the vicinity of the upper limit of the coal fluidized bed formed in the melter gasifier. In this way, it is also possible to supply the sponge iron particles with the braked vertical speed component, either by a corresponding deflection by means of projections arranged in a cascade in the lower region of the downpipe or by at least one baffle plate below the downpipe, which is preferably in the form of a blunt cone similar to a Chinese hat is.

Für eine dosierte Zufuhr der Eisenschwammpartikel in den Einschmelzvergaser ist es zweckmäßig zwischen dem Grobkornabscheider und dem Einschmelzvergaser eine Austragvorrichtung vorzusehen, durch die das Fallrohr oder die Fallrohre in gesteuerter Menge mit Eisenschwammpartikeln beliefert werden. Auf diese Weise läßt sich auch der Strömungswiderstand für das über das Fallrohr hochsteigende Reduktionsgas erhöhen und eine Überhitzung und Sinterung der Eisenschwammpartikel im Bereich des Grobkornabscheiders und im unteren Teil des Reduktionsaggregates vermeiden.For a metered supply of the sponge iron particles into the melter gasifier, it is expedient to provide a discharge device between the coarse grain separator and the melter gasifier, through which the downpipe or the downpipes are supplied in a controlled amount with sponge iron particles. In this way, the flow resistance for the reducing gas rising via the downpipe can also be increased and overheating and sintering of the sponge iron particles in the area of the coarse grain separator and in the lower part of the reduction unit can be avoided.

Die Erfindung wird durch zwei Ausführungsbeispiele anhand von vier Figuren näher erläutert. Es zeigen :

  • Figur 1 eine schematische Darstellung einer ersten Ausführungsform eines Verfahrens und einer Anlage gemäß dieser Erfindung,
  • Figur 2 in einem Längsschnitt die Ausbildung eines Fallrohres mit Flüssigkeitskühlung,
  • Figur 3 die schematische Darstellung eines Grobkornabscheiders, und
  • Figur 4 eine schematische Darstellung einer zweiten Ausführungsform eines Verfahrens und einer Anlage gemäß dieser Erfindung.
The invention is explained in more detail by two exemplary embodiments with reference to four figures. Show it :
  • FIG. 1 shows a schematic representation of a first embodiment of a method and a plant according to this invention,
  • FIG. 2 shows in a longitudinal section the formation of a downpipe with liquid cooling,
  • Figure 3 is a schematic representation of a coarse grain separator, and
  • Figure 4 is a schematic representation of a second embodiment of a method and a plant according to this invention.

Die in Fig. 1 schematisch dargestellte Anlage zur direkten Erzeugung von flüssigem Roheisen aus stückigem Eisenerz enthält einen Einschmelzvergaser 1 der in der EP-B1-0010627 beschriebenen Art. Oberhalb des Einschmelzvergasers ist ein Schachtofen 2 angeordnet, der entsprechend seiner Funktionsweise mit dem oberen Teil eines Hochofens oder eines Direktreduktionsschachtofens verglichen werden kann. Letzterer ist im Prinzip beispielsweise in der DE-A-29 35 707 beschrieben. Dem Direktreduktionsschachtofen wird von oben stückiges Eisenerz zugeführt - durch einen Pfeil 3 angedeutet -, das in Form einer losen Schüttung im Schachtofen absinkt und mittels eines über einen mittleren Gaseinlaß 4 eingeblasenen heißen Reduktionsgases einer Temperatur von etwa 750° und 900 °C zu Eisenschwamm reduziert wird. Das verbrauchte Reduktionsgas, im folgenden Gichtgas genannt, verläßt den Schachtofen 2 über einen oberen Gasauslaß 5.The plant shown schematically in Fig. 1 for the direct production of molten pig iron from lumpy iron ore contains a melter gasifier 1 of the type described in EP-B1-0010627. Above the melter gasifier, a shaft furnace 2 is arranged, which according to its mode of operation with the upper part of a Blast furnace or a direct reduction shaft furnace can be compared. The latter is described in principle, for example, in DE-A-29 35 707. Pieces of iron ore are fed to the direct reduction shaft furnace from above - indicated by an arrow 3 - which sinks in the shaft furnace in the form of a loose bed and is reduced to sponge iron by means of a hot reducing gas at a temperature of about 750 ° and 900 ° C. which is blown in via a central gas inlet 4 . The used reducing gas, hereinafter called blast furnace gas, leaves the shaft furnace 2 via an upper gas outlet 5.

Der durch Reduktion des stückigen Eisenerzes erzeugte heiße Eisenschwamm wird mit einer Temperatur von etwa 750° bis 850 °C unten aus dem Direktreduktionsschachtofen 2 ausgetragen . und gelangt über ein Rohr 6 in einen Grobkornabscheider 7. Dieser ist, wie anhand von Fig.3 näher beschrieben, ausgebildet. Alternativ enthält er ein thermisch belastbares Sieb einer Maschenweite von z. B. 12 mm, durch das Eisenschwammpartikel mit einer Größe von mehr als 12 mm zurückgehalten werden. Es erfolgt eine Trennung in eine Feinkornfraktion und eine Grobkornfraktion. Die Eisenschwammpartikel der Feinkornfraktion verlassen den Grobkornabscheider 7 über eine erste Austrittsöffnung 8 und gelangen über ein Rohr 9 in eine Austragvorrichtung 10, die beispielsweise einen Räumer oder eine Schnecke enthält. Die Eisenschwammpartikel der Grobkornfraktion verlassen den Grobkornabscheider 7 durch eine zweite Austrittsöffnung 11 und gelangen über ein Rohr 12 zu einem Kühlaggregat 13, in dem sie bis auf Raumtemperatur herabgekühlt werden, so daß sie ohne große Reoxidationsgefahr an die Stelle weitertransportiert werden können, an der sie verarbeitet werden sollen. Der Austritt der gekühlten Eisenschwammpartikel aus dem Kühlaggregat 13 ist mit 14 bezeichnet.The hot sponge iron produced by reduction of the lumpy iron ore is discharged from the direct reduction shaft furnace 2 at a temperature of approximately 750 ° to 850 ° C. and passes through a pipe 6 into a coarse grain separator 7. This is designed as described in more detail with reference to FIG. Alternatively, it contains a thermally resilient sieve with a mesh size of z. B. 12 mm, are retained by the sponge iron particles with a size of more than 12 mm. There is a separation into a fine grain fraction and a coarse grain fraction. The sponge iron particles of the fine grain fraction leave the coarse grain separator 7 via a first outlet opening 8 and pass through a pipe 9 into a discharge device 10 which contains, for example, a scraper or a screw. The sponge iron particles of the coarse grain fraction leave the coarse grain separator 7 through a second outlet opening 11 and reach a cooling unit 13 via a pipe 12, in which they are cooled down to room temperature, so that they can be transported to the point at which they are processed without great risk of reoxidation should be. The exit of the cooled sponge iron particles from the cooling unit 13 is denoted by 14.

Die Austragvorrichtung 10 weist am unteren Ende eine Austrittsöffnung 16 für die Eisenschwammpartikel auf, die überwenigstens ein Fallrohr 17 mit dem Innenraum des Einschmelzvergasers 1 in Verbindung steht. Die Eisenschwammpartikel werden über die Austrittsöffnung 16 dosiert abgegeben. Auf diese Weise werden die für den Einschmelzvergaser erforderlichen Einsatzmaterialien kontinuierlich oder intermittierend in der für den Einschmelzprozeß erforderliche Menge über das Fallrohr 17 zugegeben. Die zur Bildung und Aufrechterhaltung des Kohlefließbettes erforderliche Kohlemenge wird dem Einschmelzvergaser über ein Rohr 15 direkt zugegeben.The discharge device 10 has at the lower end an outlet opening 16 for the sponge iron particles, which at least one down pipe 17 is connected to the interior of the melter gasifier 1. The sponge iron particles are dispensed in a metered manner via the outlet opening 16. In this way, the feed materials required for the melter gasifier are added continuously or intermittently in the amount required for the melter process via the downpipe 17. The amount of coal required to form and maintain the coal fluidized bed is added directly to the melter gasifier via a pipe 15.

Wie in der EP-B1-0 010 627 beschrieben, kann der Einschmelzvergaser im Betriebszustand in drei Abschnitte unterteilt werden, nämlich in einen unteren Abschnitt 18, in dem sich Roheisen und Schlacke befinden, in einen mittleren Abschnitt 19 für das Kohlefließbett und in einen erweiterten oberen Abschnitt 20, der als Beruhigungsraum dient. Gemäß einer Weiterbildung der Erfindung erfolgt die Zufuhr der Eisenschwammpartikel nicht an der Obergrenze des Beruhigungsraumes, sondern innerhalb des Beruhigungsraumes in der Nähe der Obergrenze des Kohlefließbettes 19. Dies geschieht im vorliegenden Fall dadurch, daß das Fallrohr 17 tief in den Beruhigungsraum 20 eintaucht. Auf diese Weise läßt sich die mit dem Gas aus dem Einschmelzvergaser ausgetragene Feinkornmenge, die bei dem erfindungsgemäßen Verfahren bezogen auf die Gesamtmenge an in den Einschmelzvergaser gebrachtem Eisenschwamm eine besondere Rolle spielt, stark reduzieren. Die günstigste Eintauchtiefe des Fallrohres 17 läßt sich experimentell einfach bestimmen. Zweckmäßig endet das Fallrohr kurz oberhalb der Obergrenze des Kohlefließbettes.As described in EP-B1-0 010 627, the melter gasifier can be divided into three sections in the operating state, namely into a lower section 18, in which pig iron and slag are located, into a middle section 19 for the coal fluidized bed and into an extended section upper section 20, which serves as a relaxation room. According to a further development of the invention, the sponge iron particles are not supplied at the upper limit of the calming space, but within the calming space near the upper limit of the coal fluidized bed 19. In the present case, this is done by immersing the downpipe 17 deeply into the calming space 20. In this way, the amount of fine grain discharged with the gas from the melter gasifier, which plays a special role in the process according to the invention in relation to the total amount of sponge iron brought into the melter gasifier, can be greatly reduced. The cheapest immersion depth of the downpipe 17 can be easily determined experimentally. The downpipe expediently ends just above the upper limit of the coal fluidized bed.

Die Verwendung eines oder mehrerer Fallrohre 17 ermöglicht zudem, sei es durch Umlenkung dieser Rohre am unteren Ende, sei es durch Anbringen von Prallblechen, die senkrechte Geschwindigkeitskomponente des herabfallenden Gutes wesentlich zu vermindern und damit die Verweilzeit der Eisenschwammpartikel im Kohlefließbett zu vergrößern. Wegen der hohen thermischen Beanspruchung eines in den Innenraum des Einschmelzvergasers eintauchenden Fallrohres ist es zweckmäßig, das Rohr zu kühlen. Eine Möglichkeit der Ausbildung eines solchen Fallrohres wird anhand von Fig. 2 beschrieben.The use of one or more downpipes 17 also makes it possible, either by deflecting these pipes at the lower end or by attaching baffle plates, to significantly reduce the vertical speed component of the falling material and thus to increase the residence time of the sponge iron particles in the coal fluidized bed. Because of the high thermal stress of a down pipe immersed in the interior of the melter gasifier, it is advisable to cool the pipe. One way of forming such a down pipe is described with reference to FIG. 2.

In Fig. 1 sind bei dem Einschmelzvergaser 1 noch die Rinnen 21 und 22 für den Abstich des Roheisens und der Schlacke sowie eine Düse 23 zum Einblasen eines sauerstoffhaltigen Gases schematisch angedeutet.In Fig. 1, the channels 21 and 22 for tapping the pig iron and the slag and a nozzle 23 for blowing in an oxygen-containing gas are also indicated schematically in the melter gasifier 1.

Das im Einschmelzvergaser 1 erzeugte Reduktionsgas verläßt den Einschmelzvergaser über den Auslaß 24 mit einer Temperatur von etwa 1 200 °C. Es wird von hier über die Reduktionsgasleitung 25 zum Gaseinlaß 4 des Direktreduktionsaggregates 2 weitergeleitet. Da das in das Direktreduktionsaggregat 2 eingeleitete Reduktionsgas eine Temperatur von 900 °C nicht überschreiten darf, wird den in der Leitung 25 aufsteigenden heißen Reduktionsgasstrom zur Temperatursteuerung an der Stelle 26 Kühlgas beigemischt, das über die Leitung 17 herangeführt wird. Dieses Kühlgas ist zurückgeführtes Gichtgas des Direktreduktionsaggregates 2, nachdem dieses in einem Gichtgaswäscher 28 gewaschen und gekühlt worden ist und in einem CO2-Absorptionsturm 29 der CO2-Anteil verringert worden ist. Obwohl das so aufbereitete Gichtgas bereits in dieser Form dem heißen Reduktionsgas aus dem Einschmelzvergaser zur Temperatursteuerung beigemischt werden könnte, wurde es bei dem beschriebenen Ausführungsbeispiel über den Kühler 13 geleitet und bewirkt hier im direkten Wärmeaustausch mit den Eisenschwammpartikeln der Grobkornfraktion eine Abkühlung dieser Eisenschwammpartikel. Bei diesem Wärmeaustausch erwärmt sich das aufbereitete Gichtgas auf ca. 500 °C. Es wird dann über die Leitung 27 an der Stelle 26 dem heißen Reduktionsgasstrom der Leitung 25 zugemischt, um dessen Temperatur auf einen Wert unterhalb 900 °C zu erniedrigen. Wenn in der Anlage mehr Eisenschwamm als Roheisen erzeugt werden soll, ist es erforderlich, einen Teil des aufbereiteten Gichtgases im separaten Rekuperator 31 in Parallelschaltung zum Kühlaggregat 13 vorzuwärmen, um die gewünschte Bustlegastemperatur einstellen zu können. Als Heizgas soll das unaufbereitete Gichtgas hinter dem Gichtgaswäscher 28 verwendet werden, dessen Menge vom Wärmebedarf abhängig ist. Dadurch wird auch die Anreicherung des Kreislaufgases mit inaktiven Komponenten wie N2 vermieden.The reducing gas generated in the melter gasifier 1 leaves the melter gasifier via the outlet 24 at a temperature of approximately 1200.degree. From here it is forwarded via the reducing gas line 25 to the gas inlet 4 of the direct reduction unit 2. Since the reducing gas introduced into the direct reduction unit 2 must not exceed a temperature of 900 ° C., the hot reducing gas stream rising in the line 25 for temperature control is mixed in at the point 26 with cooling gas which is supplied via the line 17. This cooling gas is recirculated top gas of the direct reduction unit 2, after it has been washed in a top gas scrubber 28 and cooled in a CO 2 absorption tower 29 of the CO 2 content has been reduced. Although the blast furnace gas prepared in this way could already be mixed with the hot reducing gas from the melter gasifier for temperature control, in the exemplary embodiment described it was passed over the cooler 13 and, in the direct heat exchange with the iron sponge particles of the coarse grain fraction, causes these iron sponge particles to cool down. During this heat exchange, the processed top gas heats up to approx. 500 ° C. It is then mixed via line 27 at point 26 into the hot reducing gas stream of line 25 in order to lower its temperature to a value below 900 ° C. If more iron sponge than pig iron is to be produced in the system, it is necessary to preheat a portion of the processed blast furnace gas in the separate recuperator 31 in parallel with the cooling unit 13 in order to be able to set the desired bus gas temperature. The unprocessed top gas behind the top gas scrubber 28, the amount of which depends on the heat requirement, is to be used as the heating gas. This also prevents the circulation gas from being enriched with inactive components such as N 2 .

Mit 30 ist in Fig. 1 ein dem CO2-Absorp- tionsturm 29 vorgeschalteter Verdichter bezeichnet, der den erforderlichen Druck erzeugt. Um Eisenschwamm mit wenig Schwefel erzeugen zu können, ist es erforderlich, das Gas aus dem Einschmelzvergaser 1 im Heißgasentschwefelungsaggregat 32 zu entschwefeln. Zu diesem Zweck kann diesem Gas etwas Kaltgas beigemischt werden, um seine Temperatur dem Entschwefelungsvorgang anzupassen.In FIG. 1, 30 denotes a compressor upstream of the CO 2 absorption tower 29, which generates the required pressure. In order to be able to produce sponge iron with little sulfur, it is necessary to desulfurize the gas from the melter gasifier 1 in the hot gas desulfurization unit 32. For this purpose, some cold gas can be added to this gas to adjust its temperature to the desulfurization process.

Zur Vermeidung einer Sinterbildung ist es erforderlich, daß die Menge der über die Rohre 17, 9 und 6 nach oben gelangenden heißen Gase aus dem Einschmelzvergaser gering gehalten wird. Dies ist durch einen hohen Strömungswiderstand im Bereich Austragsvorrichtung 10, Fallrohr 9 und Grobkornabscheider 7 möglich, wenn der Austrag so gesteuert wird, daß das Rohr 9 stets wenigstens zum Teil mit Material ausgefüllt ist. Auf diese Weise wird der Widerstand des Nebenweges zur Reduktionsgasleitung 25 so hoch gehalten, daß sich keine schädliche Gasströmung über diesen Nebenweg ausbilden kann.To avoid sintering, it is necessary that the amount of hot gases coming up through the pipes 17, 9 and 6 from the melter gasifier is kept low. This is possible due to a high flow resistance in the area of discharge device 10, downpipe 9 and coarse grain separator 7 if the discharge is controlled in such a way that the pipe 9 is always at least partially filled with material. In this way, the resistance of the secondary path to the reducing gas line 25 is kept so high that no harmful gas flow can form over this secondary path.

In Fig. ist der in den Einschmelzvergaser eintauchende Teil eines Fallrohres 17 im Schnitt dargestellt. Wegen der hohen thermischen Beanspruchung im Inneren des Einschmelzvergasers ist das Fallrohr mit einer Flüssigkeitskühlung versehen. Zu diesem Zweck wird durch drei konzentrisch zueinander angeordnete Metallrohre 31, 32 und 33 in der dargestellten Weise ein Flüssigkeitskanal gebildet, durch den eine Kühlflüssigkeit beispielsweise Wasser hindurchgeleitet wird. Das Kühlsystem ist allseitig mit einer feuerfesten Schicht 34 bedeckt.In Fig. The part of a down pipe 17 immersed in the melter gasifier is shown in section. Because of the high thermal stress inside the melter gasifier, the downpipe has a liquid cooling system Mistake. For this purpose, a liquid channel is formed by three metal tubes 31, 32 and 33 arranged concentrically to one another, through which a cooling liquid, for example water, is passed. The cooling system is covered on all sides with a refractory layer 34.

Das dargestellte Fallrohr 17 enthält Maßnahmen durch Umlenkung die Vertikalgeschwindigkeit der herabfallenden Eisenschwammpartikel zu verringern und damit wegen der verringerten Eintrittsgeschwindigkeit in das Kohlefließbett hier die Verweilzeit zu erhöhen. Zu diesem Zweck sind im unteren Bereich des Fallrohres kaskadenförmig angeordnete Vorsprünge 35 vorgesehen, auf denen sich Material ablagern kann, das dadurch als Verschleißschutz dient. Anstelle dieser Vorsprünge oder zusätzlich zu diesen Vorsprüngen kann auch an der unteren Austrittsöffnung des Rohres ein Prallblech 36, vorzugsweise in Form eines stumpfen Kegels ähnlich einem Chinesenhut, vorgesehen sein. Die herabfallenden Eisenschwammpartikel werden durch die Vorsprünge 35 im Rohr mäanderförmig abgelenkt und abgebremst und durch das Prallblech 36 etwa in eine horizontale Richtung abgelenkt, wodurch ihre vertikale Geschwindigkeitskomponente beträchtlich verringert wird. Mit 37 ist in Fig. 2 die Decke des Einschmelzvergasers bezeichnet.The downpipe 17 shown contains measures by deflection to reduce the vertical speed of the falling sponge iron particles and thus to increase the dwell time here because of the reduced entry speed into the coal fluidized bed. For this purpose, cascade-shaped projections 35 are provided in the lower region of the downpipe, on which material can deposit, which thereby serves as wear protection. Instead of these projections or in addition to these projections, a baffle plate 36, preferably in the form of a blunt cone similar to a Chinese hat, can also be provided at the lower outlet opening of the tube. The falling sponge iron particles are deflected and braked in a meandering manner by the projections 35 in the tube and deflected approximately in a horizontal direction by the baffle plate 36, as a result of which their vertical speed component is considerably reduced. The ceiling of the melter gasifier is designated by 37 in FIG. 2.

Der in Fig. 3 schematisch dargestellte Grobkornabscheider 7 ist in Form einer schrägen Fallrinne 38 mit wenigstens einem von dieser nach unten abzweigenden Stutzen 39 ausgebildet. Entsprechend Fig. 1 ist das Rohr über das die aus dem Direktreduktionsschachtofen ausgetragenen Eisenschwammpartikel zugeführt werden mit 6 bezeichnet, die erste Austrittsöffnung für die Feinkornfraktion mit 8 und die zweite Austrittsöffnung für die Grobkornfraktion mit 11.The coarse-grain separator 7 shown schematically in FIG. 3 is designed in the form of an inclined gutter 38 with at least one connecting piece 39 branching off from it. According to FIG. 1, the pipe through which the sponge iron particles discharged from the direct reduction shaft furnace are fed is designated by 6, the first outlet opening for the fine-grain fraction is 8 and the second outlet opening for the coarse-grain fraction is 11.

Das von oben in den Grobkornabscheider 7 eintretende Schüttgut wird während der Bewegung durch den Grobkornabscheider natürlich entmischt, d. h. die feinen Partikel setzen sich nach unten ab und die groben sammeln sich an der Oberseite. Bei geeigneter Steuerung des Abzugs der Eisenschwammpartikel der Feinkornfraktion aus der ersten Austrittsöffnung 8 erhält man das in Fig. 3 schematisch dargestellte Fließprofil, d. h. die groben Eisenschwammpartikel werden im wesentlichen über das Fallrohr 38 zur zweiten Austrittsöffnung 12 weitergeleitet und von dort abgezogen. Erfolgt die Steuerung des Abzugs der feinen Eisenschwammpartikel entsprechend Fig. 1 durch eine Austragsvorrichtung 10, die über ein Rohr mit dem Grobkornabscheider 7 verbunden ist, dann läßt sich, wie gewünscht, der Strömungswiderstand für das aus dem Einschmelzvergaser hochsteigende Gas verhältnismäßig hoch halten.The bulk material entering the coarse grain separator 7 from above is naturally separated during the movement by the coarse grain separator, i. H. the fine particles settle down and the coarse particles collect on the top. With a suitable control of the removal of the sponge iron particles of the fine grain fraction from the first outlet opening 8, the flow profile shown schematically in FIG. H. the coarse iron sponge particles are essentially passed on via the downpipe 38 to the second outlet opening 12 and drawn off from there. 1 is controlled by a discharge device 10, which is connected via a tube to the coarse grain separator 7, then, as desired, the flow resistance for the gas rising from the melter gas can be kept relatively high.

Bei der schematischen Darstellung einer zweiten Ausführungsform einer Anlage nach Fig.4 sind die mit der Anlage nach Fig. 1 übereinstimmenden Teile durch dieselben Bezugszeichen gekennzeichnet.In the schematic representation of a second embodiment of a system according to FIG. 4, the parts which correspond to the system according to FIG. 1 are identified by the same reference numerals.

Ein als Direktreduktionsschachtofen 2 ausgebildetes Direktreduktionsaggregat weist oben eine Eintragvorrichtung 3 für das stückige Eisenerz und einen Gasauslaß 5 für das verbrauchte Reduktionsgas (Gichtgas) und unten eine steuerbare Austragvorrichtung 41 für die durch Direktreduktion aus dem Eisenerz gewonnenen Eisenschwammpartikel sowie einen Gaseinlaß 4 für heißes Reduktionsgas auf. Der Einschmelzvergaser 1 entspricht im wesentlichen dem Einschmelzvergaser der ersten Ausführungsform. Die Decke des als Beruhigungsraum dienenden oberen Abschnittes 20 weist hier jedoch eine als Vergaserkopf 42 bezeichnete Kammer auf, die mit dem Beruhigungsraum in Verbindung steht. Im Vergaserkopf ist ein Gasauslaß 43 für das im Einschmelzvergaser erzeugte Reduktionsgas (Rohgas), ein Gaseinlaß 44 für gewaschenes und aufbereites Gichtgas des Direktreduktionsschachtofens sowie ein Einlaß 45 für ein Entschwefelungsmittel vorgesehen. Durch die Decke des Einschmelzvergasers sind außerdem das Rohr 15 für die Zugabe von Kohle und das Tauchrohr 17 für die Zugabe der Feinkornfraktion durchgeführt.A direct reduction shaft unit designed as a direct reduction shaft furnace 2 has an inlet device 3 for the lumpy iron ore and a gas outlet 5 for the used reducing gas (top gas) and a controllable discharge device 41 for the iron sponge particles obtained by direct reduction from the iron ore and a gas inlet 4 for hot reducing gas. The melter gasifier 1 essentially corresponds to the melter gasifier of the first embodiment. However, the ceiling of the upper section 20 serving as a calming space here has a chamber called a carburetor head 42, which is in communication with the calming space. Provided in the gasifier head is a gas outlet 43 for the reducing gas (raw gas) generated in the melter gasifier, a gas inlet 44 for scrubbed and treated top gas from the direct reduction shaft furnace, and an inlet 45 for a desulfurizing agent. The pipe 15 for the addition of coal and the immersion pipe 17 for the addition of the fine grain fraction are also carried out through the ceiling of the melter gasifier.

Im unteren Bereich des Einschmelzvergasers sind Auslässe 21 für flüssiges Roheisen sowie 22 für flüssige Schlacke, ferner oberhalb des Schlackenspiegels wenigstens eine Düse 23 bzw. wenigstens ein Brenner 23a für das Einblasen von Gasen und feinkörnigen Feststoffen vorgesehen.Outlets 21 for liquid pig iron and 22 for liquid slag are provided in the lower region of the melting gasifier, furthermore at least one nozzle 23 or at least one burner 23a is provided above the slag level for blowing in gases and fine-grained solids.

Unterhalb des Direktreduktionsschachtofens 2 befindet sich ein Kühlaggregat 13a für die durch die Austragvorrichtung 41 ausgetragenen heißen Eisenschwammpartikel. Die Eintrittsöffnung 46 des Kühlaggregates 13a für die heißen Eisenschwammpartikel steht durch die Fallrohrleitung 6 mit der Austragvorrichtung 41 in Verbindung. Der Fallrohrleitung 6 ist eine Niveaumeßeinrichtung 47 zugeordnet, durch die die Austragvorrichtung 41 steuerbar ist.Below the direct reduction shaft furnace 2 there is a cooling unit 13a for the hot sponge iron particles discharged by the discharge device 41. The inlet opening 46 of the cooling unit 13a for the hot sponge iron particles is connected to the discharge device 41 through the downpipe 6. The down pipe 6 is assigned a level measuring device 47, by means of which the discharge device 41 can be controlled.

Das Kühlaggregat 13a weist im oberen Bereich neben der Eintrittsöffnung 46 für die heißen Eisenschwammpartikel einen Auslaß 48 für das Kühlgas und im unteren Bereich neben einer Austrittsöffnung 14 für die gekühlten Eisenschwammpartikel einen Einlaß 49 für das Kühlgas auf. Die Kühlung erfolgt wie bei dem Ausführungsbeispiel nach Fig. 1 im Gegenstrom und im direkten Austausch mit den im Kühlaggregat absinkenden Eisenschwammpartikeln. Da dem Kühlaggregat 13a nicht nur, wie bei dem Ausführungsbeispiel nach Fig. 1, die Grobkornfraktion der Eisenschwammpartikel zugeführt wird, ist es zweckmäßig, das Kühlaggregat im oberen Bereich mit einem Beruhigungsraum zu versehen, um den Austrag an Feinteilen möglichst gering zu halten. Dies kann beispielsweise dadurch geschehen, daß das Fallrohr 6 in einer bestimmten Länge in das Kühlaggregat eingeführt wird, so daß sich oberhalb des Schüttkegels innerhalb des Kühlaggregates ein Beruhigungsraum ausbildet.The cooling unit 13a has an outlet 48 for the cooling gas in the upper region next to the inlet opening 46 for the hot sponge iron particles and an inlet 49 for the cooling gas in the lower region next to an outlet opening 14 for the cooled sponge iron particles. As in the exemplary embodiment according to FIG. 1, cooling takes place in countercurrent and in direct exchange with the iron sponge particles sinking in the cooling unit. Since not only the coarse grain fraction of the iron sponge particles is fed to the cooling unit 13a, as in the embodiment according to FIG. 1, it is expedient to provide the cooling unit in the upper region with a calming space in order to keep the discharge of fine particles as low as possible. This can be done, for example, by inserting the downpipe 6 into the cooling unit in a certain length, so that a calming space is formed above the pouring cone within the cooling unit.

Unterhalb des Kühlaggregates und mit dessen Austrittsöffnung 14 durch ein weiteres Fallrohr 48 verbunden, befindet sich eine als Siebstation ausgebildete Klassiervorrichtung 7a, durch die die Trennung der Eisenschwammpartikel in eine Feinkornfraktion und in eine Grobkornfraktion bewirkt wird. Die Austrittsöffnung 8 für die Feinkornfraktion ist durch die Rohrleitung 9 mit dem oberhalb des Einschmelzvergasers angeordneten Feinkornbehälter 10 verbunden, dessen Austrittsöffnung 16 mit dem Tauchrohr 17 in Verbindung steht. Alternativ oder zusätzlich kann auch eine Verbindung zu dem Rohr 15 vorhanden sein, über das die Kohle in den Einschmelzvergaser eingeführt wird. Falls die Klassiervorrichtung 7a aus Platzmangel nicht oberhalb des Einschmelzvergasers 1 angeordnet und die Rohrleitung 9 nicht als Fallrohrleitung ausgebildet sein kann, sind in dieser Rohrleitung geeignete Fördermittel für die Feinkornfraktion vorzusehen. Erfolgt die Trennung in der Klassiervorrichtung 7a so, daß die Feinkornfraktion nur Teile mit einer Körnung bis 3 mm enthält, dann kann es zweckmäßig sein, wenigstens einen Teil dieser Fraktion über die Düsen 23 bzw. 23a in den Einschmelzvergaser einzublasen. Es sind dann entsprechende Rohrleitungen zu den Düsen vorzusehen.Below the cooling unit and with its outlet opening 14 through a further downpipe 48 connected, there is a classifying device 7a designed as a sieving station, by means of which the sponge iron particles are separated into a fine-grain fraction and a coarse-grain fraction. The outlet opening 8 for the fine-grain fraction is connected by the pipeline 9 to the fine-grain container 10 arranged above the melter gasifier, the outlet opening 16 of which is connected to the dip tube 17. Alternatively or additionally, there may also be a connection to the pipe 15 via which the coal is introduced into the melter gasifier. If the classifying device 7a is not arranged above the melter gasifier 1 due to lack of space and the pipeline 9 cannot be designed as a downpipe, suitable conveying means for the fine-grain fraction must be provided in this pipeline. If the separation takes place in the classifying device 7a in such a way that the fine-grain fraction contains only parts with a grain size of up to 3 mm, then it may be expedient to blow at least part of this fraction into the melter gasifier via the nozzles 23 and 23a. Appropriate pipelines to the nozzles must then be provided.

Mit der Austrittsöffnung 11 der Klassiervorrichtung 7a für die Grobkornfraktion, die aus dem Verfahren ausgeschieden wird, ist eine Rohrleitung 12 verbunden, durch die die Grobkornfraktion einem gesonderten Einschmelzaggregat oder einer Einrichtung zum Kompaktieren, Passivieren oder auch einem weiteren Kühlaggregat 13 entsprechend Fig. 1 zuführbar ist, dem aufbereitetes Gichtgas als Kühlmedium zugeführt wird.A pipe 12 is connected to the outlet opening 11 of the classifying device 7a for the coarse grain fraction, which is excreted from the process, through which the coarse grain fraction can be fed to a separate melting unit or a device for compacting, passivating or also a further cooling unit 13 according to FIG. 1 , to which the processed blast furnace gas is fed as a cooling medium.

Wie bei dem Ausführungsbeispiel nach Fig. 1 ist ein Gichtgaswäscher 28 mit dem Gichtgasauslaß 5 des Direktreduktionsschachtofens verbunden, und der Gasauslaß 51 des Gichtgaswäschers 28 steht über Rohrleitungen 52 und 53 mit einem CO2-Absorptionsturm 29 in Verbindung, dessen Gasauslaß 54 über Leitungen 55 und 56 mit dem Einlaß 49 des Kühlaggregates 13a für das Kühlgas verbunden ist. Außerdem ist, wie bei dem ersten Ausführungsbeispiel, eine Rohrleitung 27 vom Gasauslaß 48 des Kühlaggregates 13a zur Reduktionsgasleitung 25 vorgesehen, um dem über diese Leitung zum Gaseinlaß 4 des Direktreduktionsschachtofens 2 geführten Reduktionsgasstrom aufbereitetes und im Kühlaggregat 13a erwärmtes Gichtgas beizumischen. Hierdurch wird nicht nur eine Temperatursteuerung des dem Direktreduktionsschachtofen 2 zugeführten Reduktionsgases ermöglicht, sondern es kann der Kohle- und Sauerstoffverbrauch im Einschmelzvergaser nahezu auf die Hälfte reduziert werden. Dadurch wird auch die mit Kohle eingetragene Schwefelmenge und der Schwefelgehalt im Reduktionsgas auf ca. die Hälfte reduziert.1, a top gas scrubber 28 is connected to the top gas outlet 5 of the direct reduction shaft furnace, and the gas outlet 51 of the top gas scrubber 28 is connected via pipes 52 and 53 to a CO 2 absorption tower 29, whose gas outlet 54 is connected via lines 55 and 56 is connected to the inlet 49 of the cooling unit 13a for the cooling gas. In addition, as in the first exemplary embodiment, a pipeline 27 is provided from the gas outlet 48 of the cooling unit 13a to the reducing gas line 25 in order to admix the blast furnace gas which has been processed and heated in the cooling unit 13a with the reducing gas stream which is conducted via this line to the gas inlet 4 of the direct reduction shaft furnace 2. This not only enables temperature control of the reducing gas supplied to the direct reduction shaft furnace 2, but also the coal and oxygen consumption in the melter gasifier can be reduced by almost half. This also reduces the amount of sulfur introduced with coal and the sulfur content in the reducing gas to about half.

Ergänzend zu der Anlage nach Fig. 1 sind bei der Anlage nach Fig. 4 noch die folgenden Vorrichtungen und Verbindungsleitungen vorgesehen.In addition to the system according to FIG. 1, the following devices and connecting lines are also provided in the system according to FIG. 4.

Dem Kühlaggregat 13a ist ein die Rohrleitung 56 enthaltender Kühlgaskreislauf 57 mit einem Kühlgaswäscher 58 und einem Kompressor 30a zugeordnet. Hierdurch wird der Tatsache Rechnung getragen, daß für die Kühlung im Kühlaggregat eine größere Kühlgasmenge benötigt wird, als aufbereitetes, über die Rohrleitung 55 zugeführtes Gichtgas zur Verfügung steht.The cooling unit 13a is assigned a cooling gas circuit 57 containing the pipeline 56 with a cooling gas scrubber 58 and a compressor 30a. This takes into account the fact that a larger amount of cooling gas is required for cooling in the cooling unit than processed top gas supplied via the pipeline 55 is available.

Von der Rohrleitung 27, die mit dem Gasauslaß 48 des Kühlaggregates bzw. dem Kühlgaskreislauf 57 verbunden ist, zweigt eine Rohrleitung 59 zum Einlaß 44 im Vergaserkopf 42 ab, in die eine Verbindungsleitung 60 zum Gasauslaß 54 des CO2-Absorptionsturms 29 mündet. Über die Rohrleitung 59 kann dem Vergaserkopf 42 aufbereitetes Gichtgas unterschiedlicher Temperatur zugeführt werden, so daß hier die Temperatur auf eine für die Heißgasentschwefelung optimale Temperatur einstellbar ist.From the pipeline 27, which is connected to the gas outlet 48 of the cooling unit or the cooling gas circuit 57, a pipeline 59 branches off to the inlet 44 in the carburetor head 42, into which a connecting line 60 to the gas outlet 54 of the CO 2 absorption tower 29 opens. Treated top gas of different temperatures can be supplied to the gasifier head 42 via the pipeline 59, so that the temperature can be set here to an optimum temperature for the hot gas desulfurization.

Der Auslaß 43 im Vergaserkopf 42 für das im Einschmelzvergaser 1 erzeugte Reduktionsgas ist über eine Rohrleitung 61 mit einem Zyklon 62 verbunden, an dessen Gasauslaß 63 die zum Direktreduktionsaggregat führende Reduktionsgasleitung 25 angeschlossen ist. Anstelle eines Zyklons können auch mehrere zu einer Zyklonbatterie zusammengeschaltete Zyklone eingesetzt werden. Die Austrittsöffnung 64 für die ausgeschiedenen Feststoffe steht durch eine Rohrleitung 65 mit einer Rohrleitung 66 in Verbindung, die über einen Kompressor 30 mit dem Gasauslaß 51 des Gichtgaswäschers 28 verbunden ist. Die Rohrleitung 66 führt einen Teil des den Gichtgaswäscher 28 verlassenden Gichtgases dem Brenner 23a als sauerstoffhaltiges Gas zu, wobei dieses Gas zugleich als Trägergas für die ausgeschiedenen Feststoffe des Zyklons 62 dient. Dem Brenner 23a bzw. den Düsen 23 ist außerdem über eine Rohrleitung 67 Sauerstoff zuführbar. Eine Zweigleitung 68 führt von der mit dem Gasauslaß 51 des Gichtgaswäschers 28 verbundene Rohrleitung 52 zu einem Dampferzeuger 69. Ein Teil des unaufbereiteten Gichtgases kann so als Heizgas für die Erzeugung von Dampf verwendet werden, der im CO2-Absorptionsturm 29 benötigt wird.The outlet 43 in the gasifier head 42 for the reducing gas generated in the melter gasifier 1 is connected via a pipeline 61 to a cyclone 62, to the gas outlet 63 of which the reducing gas line 25 leading to the direct reduction unit is connected. Instead of one cyclone, it is also possible to use several cyclones connected to form a cyclone battery. The outlet opening 64 for the separated solids is connected by a pipeline 65 to a pipeline 66 which is connected via a compressor 30 to the gas outlet 51 of the top gas scrubber 28. The pipeline 66 feeds part of the top gas leaving the top gas scrubber 28 to the burner 23a as an oxygen-containing gas, this gas also serving as a carrier gas for the separated solids of the cyclone 62. Oxygen can also be supplied to the burner 23a or the nozzles 23 via a pipeline 67. A branch line 68 leads from the pipeline 52 connected to the gas outlet 51 of the top gas scrubber 28 to a steam generator 69. A part of the untreated top gas can thus be used as heating gas for the generation of steam which is required in the CO 2 absorption tower 29.

Bei dem mit der Anlage nach Fig. 4 durchgeführten Verfahren ist neben der Forderung, eine Überschußmenge an im Einschmelzvergaser 1 erzeugtem Reduktionsgas zu vermeiden, in besonders wirtschaftlicher Weise auch die Forderung berücksichtigt, den Schwefelgehalt des im Einschmelzvergaser erschmolzenen Roheisens und in der aus dem Verfahren ausgeschiedenen Grobkornfraktion der Eisenschwammpartikel niedrig zu halten, wenn als Energieträger stark schwefelhaltige Kohle eingesetzt wird.In the process carried out with the plant according to FIG. 4, in addition to the requirement to avoid an excess amount of reducing gas generated in the melter gasifier 1, the requirement is also taken into account in a particularly economical manner, the sulfur content of the pig iron melted in the melter gasifier and that removed from the process To keep the coarse grain fraction of the iron sponge particles low if coal with a high sulfur content is used as an energy source.

Zu diesem Zweck werden Maßnahmen vorgesehen, um den für das Einschmelzen der Feinkornfraktion im Einschmelzvergaser erforderlichen Energieanteil zu verringern und das Gichtgas des Direktreduktionsaggregates teilweise im unaufbereiteten Zustand, teilweise nach einer C027Wäsche und nach direktem Wärmeaustausch im Kühlaggregat für die aus dem Direktreduktionsaggregat ausgetragenen Eisenschwammpartikel dem Prozeß zuzuführen.For this purpose, measures are provided to reduce the amount of energy required for melting the fine grain fraction in the melter gasifier and the blast furnace gas of the direct reduction unit partly in the unprocessed state, partly after a C0 2 7 wash and after direct heat exchange in the cooling unit for the iron sponge particles discharged from the direct reduction unit Process.

Der für die Schmelzwärme erforderliche, durch Verbrennung von Kohle aufzubringende Energieanteil wird dadurch vermindert, daß bei der Trennung der Eisenschwammpartikel in der Klassiervorrichtung 7a der Anteil der Freinkornfraktion gegenüber der Grobkornfraktion vermindert, d. h. das Kornband der dem Einschmelzvergaser 1 zugeführten Feinkornfraktion auf Teilchen bis zu einer Größe von 5 mm, vorzugsweise 3 mm, reduziert wird. Diese Teilchen lassen sich wegen der längeren Verweilzeit in der Wirbelschicht des Einschmelzvergasers mit einem wesentlich niedrigeren Energieaufwand, d. h. also mit weniger Kohle und damit weniger Schwefel erschmelzen. Es ist dann auch möglich, einen Teil des vom Gichtgaswäscher 28 gelieferten unaufbereiteten Gichtgases, das Kohlendioxid und Wasserdampf enthält, zum Vergasen der Kohle einzusetzen. Bei dem Ausführungsbeispiel nach Fig. 4 wird ein Teil des Gichtgases über die Leitung 66 einem oder mehreren Brennern 23a des Einschmelzvergasers 1 zugeführt, die in das Kohlefließbett münden. Mit dem Gichtgas als Trägergas wird auch der Austrag des Zyklons 62, nämlich aus dem Reduktionsgas ausgeschiedene Kohlepartikel und Entschwefelungsmittel, in den Einschmelzvergaser zurückgeführt. Um die Einblasöffnung vom Verschlacken freizuhalten, wird dem Brenner über die Leitung 67 Sauerstoff oder Luft als Verbrennungsmittel zugeführt und ein Teil des Gichtgases bzw. des Gichtgas-Staubgemisches verbrannt. Die über die Rohrleitung 66 zugeführte Gichtgasmenge soll so eingestellt werden, daß die Vergaserkopftemperatur in Verbindung mit anderen Temperatursteuerungsmaßnahmen zwischen 850° und 1 250 °C, vorzugsweise bei 1 100°C liegt. Durch die mögliche Verwendung von Gichtgas als Sauerstoffträger für die Durchführung der Vergasung läßt sich selbstverständlich auch der Sauerstoffverbrauch pro Tonne Produkt erniedrigen und damit die Wirtschaftlichkeit des Verfahrens erhöhen.The proportion of energy required by the combustion of coal for the heat of fusion is reduced in that, when the sponge iron particles are separated in the classifying device 7a, the proportion of the free-grain fraction is reduced compared to the coarse-grain fraction, i. H. the grain band of the fine-grain fraction fed to the melter gasifier 1 is reduced to particles up to a size of 5 mm, preferably 3 mm. Because of the longer dwell time in the fluidized bed of the melter gasifier, these particles can be consumed with a significantly lower energy expenditure, i. H. so melt with less coal and therefore less sulfur. It is then also possible to use a portion of the unprocessed top gas supplied by the top gas scrubber 28, which contains carbon dioxide and water vapor, for gasifying the coal. In the exemplary embodiment according to FIG. 4, part of the blast furnace gas is fed via line 66 to one or more burners 23a of the melter gasifier 1, which open into the coal fluidized bed. With the blast furnace gas as the carrier gas, the discharge of the cyclone 62, namely carbon particles and desulphurizing agent separated from the reducing gas, is also returned to the melter gasifier. In order to keep the blow-in opening free of slagging, oxygen or air is fed to the burner via line 67 as a combustion medium and part of the blast furnace gas or the blast furnace gas / dust mixture is burned. The amount of blast furnace gas supplied via the pipeline 66 should be set so that the carburetor head temperature in connection with other temperature control measures is between 850 ° and 1 250 ° C, preferably at 1 100 ° C. The possible use of blast furnace gas as an oxygen carrier for carrying out the gasification can of course also reduce the oxygen consumption per ton of product and thus increase the economics of the process.

Eine weitere Einsparung an Kohle und damit eine weitere Reduzierung des Schwefelgehalts im Reduktionsgas und im Eisenschwamm läßt sich dadurch erzielen, daß im C027Absorptionsturm aufbereitetes Gichtgas dem Reduktionsgas beigemischt wird. Dies geschieht bei dem Verfahren mit der Anlage nach Fig. 4 dadurch, daß ein Teil des im CO2-Absorptionsturm 29 aufbereiteten Gichtgases über die Rohrleitungen 55 und 56 durch das Kühlaggregat 13a geleitet wird, dieser Teil sich im direkten Kontakt mit den heißen Eisenschwammpartikeln erwärmt und dann wiederum ein Teil hiervon der Reduktionsgasleitung 25 und ein weiterer Teil über die Rohrleitung 59 dem Vergaserkopf 42 zugeführt wird. Der andere Teil des vom C027Absorptionsturm gelieferten aufbereiteten Gichtgases wird unmittelbar über die Rohrleitung 60 und einem Teil der Rohrleitung 59 dem Vergaserkopf 42 zugeführt. Durch die dem Reduktionsgas beigemischte Menge an aufbereitetem Gichtgas kann der Kohle- und Sauerstoffverbrauch und damit die mit Kohle eingetragene Schwefelmenge und der Schwefelgehalt im Reduktionsgas auf ca. die Hälfte reduziert werden.A further saving in coal and thus a further reduction in the sulfur content in the reducing gas and in the sponge iron can be achieved in that blast furnace gas processed in the CO 2 absorption tower is mixed with the reducing gas. 4 in that part of the blast furnace gas processed in the CO 2 absorption tower 29 is passed via the pipes 55 and 56 through the cooling unit 13a, this part heats up in direct contact with the hot sponge iron particles and then again a part thereof is fed to the reducing gas line 25 and a further part to the carburetor head 42 via the pipeline 59. The other part of the processed top gas supplied by the C0 2 7 absorption tower is fed directly to the gasifier head 42 via the pipe 60 and part of the pipe 59. The amount of processed blast furnace gas mixed with the reducing gas can reduce the consumption of coal and oxygen, and thus the amount of sulfur introduced with coal, and the sulfur content in the reducing gas to about half.

Mit dem über die Rohrleitung 59 dem Vergaserkopf 42 zugeführten, aufbereiten Gichtgas wird auch eine Temperatursteuerung vorgenommen, wobei die Temperatur in der Leitung 59 durch den Anteil der über die Rohrleitung 27 und über die Rohrleitung 60 zugeführten Mengen bestimmt werden kann. Die Temperatureinstellung im Vergaserkopf ist insbesondere dann wesentlich, wenn diesem oder der Abgasleitung 61 ein Entschwefelungsmittel zugeführt wird; um den Schwefelgehalt im Reduktionsgas weiter zu senken. Die optimale Temperatur für eine Heißgasentschwefelung liegt bei ca. 900 °C. Bei dem beschriebenen Verfahren wird dem Vergaserkopf 42 über die Öffnung 45 ein Entschwefelungsmittel, wie Kalkhydrat, in feinkörniger Form zugeführt und die für die Heißgasentschwefelung optimale Temperatur durch das durch den Gaseinlaß 44 eingeblasene, aufbereitete Gichtgas eingestellt. Die Entschwefelung des Reduktionsgases erfolgt im wesentlichen im Vergaserkopf und in der Abgasleitung 61. Verbrauchtes und noch nicht verbrauchtes Entschwefelungsmittel wird im Zyklon 62 ausgeschieden und über die Leitung 65 in den Einschmelzvergaser zurückgeführt.A temperature control is also carried out with the processed blast furnace gas supplied to the gasifier head 42 via the pipe 59, the temperature in the pipe 59 being able to be determined by the proportion of the quantities supplied via the pipe 27 and the pipe 60. The temperature setting in the carburetor head is particularly important when a desulfurizing agent is supplied to this or the exhaust line 61; to further reduce the sulfur content in the reducing gas. The optimal temperature for hot gas desulfurization is approx. 900 ° C. In the described method, a desulfurizing agent, such as hydrated lime, is fed to the gasification head 42 through the opening 45 in fine-grained form, and the optimum temperature for the hot gas desulfurization is set by the processed blast furnace gas blown through the gas inlet 44. The desulphurization of the reducing gas takes place essentially in the gasifier head and in the exhaust line 61. Used and not yet used desulfurization agent is separated out in the cyclone 62 and returned to the melter gasifier via line 65.

Durch die genannten Maßnahmen läßt sich auch beim Einsatz schwefelreicher Kohle der Schwefelgehalt der Eisenschwammpartikel so weit absenken, daß die ausgeschiedene Grobkornfraktion ohne weitere Maßnahmen zur Schwefelentfernung in einem Stahlwerk verarbeitet werden kann. Die Feinkornfraktion, die aus den genannten Gründen einen wesentlich höheren Schwefelgehalt als die Grobkornfraktion besitzt - wegen der im Verhältnis zum Gewicht größeren Oberfläche wird durch die feinen Eisenschwammpartikel eine größere Schwefelmenge gebunden -, wird durch die dem Einschmelzvergaser zugeführten Entschwefelungsmittel wenigstens zum Teil entschwefelt und gebunden an das Entschwefelungsmittel durch die Schlacke ausgeschieden.The measures mentioned allow the sulfur content of the iron sponge particles to be reduced so much even when using sulfur-rich coal that the coarse-grain fraction which has been separated out can be processed in a steel mill without further measures for sulfur removal. The fine grain fraction, which for the reasons mentioned has a significantly higher sulfur content than the coarse grain fraction - due to the larger surface in relation to the weight, a larger amount of sulfur is bound by the fine sponge iron particles - is desulfurized and bound at least in part by the desulfurization agent supplied to the melter gasifier the desulfurizing agent is excreted through the slag.

Claims (36)

1. Process for directly producing sponge iron particles and liquid pig iron from pieces of iron ore, in which the iron ore is reduced in a direct reduction assembly in the form of a loose filling by means of a hot reducing gas to sponge iron particles, and sponge iron particles carried out of the direct reduction assembly are fed to a melt-down gasifier, in which the heat necessary for melting the pig iron and also reduction gas are produced from introduced coal and oxygen-containing gas which is blown in of which at least a part is led after cooling to a temperature prescribed for the reduction into the reduction zone of the direct reduction assembly, characterised in that the pig iron particles carried out of the direct reduction assembly are divided into a fine grain fraction and a coarse grain fraction and only the fine grain fraction is fed to the melt-down gasifier.
2. Process according to claim 1, characterised in that the fine grain fraction contains particles up to a size of 20 mm.
3. Process according to claim 2, characterised in that the fine grain fraction contains particles up to a size of 12 mm.
4. Process according to claim 1, characterised in that the upper limit for the particle size of the fine grain fraction is so selected that the amount of the reduction gas produced by melting down the pig iron particles in the melt-down gasifier corresponds roughly to the amount required for the reduction process for the iron ore in the direct reduction assembly.
5. Process according to any of claims 1 to 4, characterised in that the pig iron particles of the fine grain fraction adjacent to the upper face of the fluidized bed formed in the melt-down gasifier are fed with limited vertical component of velocity.
6. Process according to claim 5, characterised in that the pig iron particles are fed in by at least one tube.
7. Process according to any of claims 1 to 6, characterised in that the division between fine grain fraction and coarse grain fraction is so selected that the average sulphur content of the fine grain fraction amounts to at least five times the average sulphur content of the coarse grain fraction.
8. Process according to claim 2, characterised in that the average sulphur content of the fine grain fraction amounts to at least ten times the average sulphur content of the coarse grain fraction.
9. Process according to claims 7 and 8, characterised in that the fine grain fraction contains a substantial proportion of particles up to a size of 5 mm.
10. Process according to claim 9 characterised in that the fine grain fraction contains a substantial proportion of particles up to a size of 3 mm.
11. Process according to any of claims 1 to 10 characterised in that the reduction gas produced in the melt-down gasifier is fed with a sulphur extraction agent.
12. Process according to claim 11, characterised in that the sulphur extraction agent is blown into the head and/or the exhaust duct of the melt-down gasifier for the reduction gas.
13. Process according to any of claims 1 to 12 characterised in that a part of the top gas of the direct reduction assembly is mixed with the reduction gas produced in the melt-down gasifier, after being scrubbed in a top gas scrubber and cooled and prepared by extracting CO2,
14. Process according to claim 13, characterised in that at least a part of the scrubbed and prepared top gas is heated by direct heat exchange with sponge iron particles being carried out of the direct reduction assembly, before it is mixed with the reduction gas.
15. Process according to claim 13 or 14, characterised in that the prepared top gas is blown into the head of the melt-down gasifier.
16. Process according to claim 13 to 15, characterised in that the prepared top gas is blown into the reduction gas duct between the melt-down gasifier and the direct reduction assembly.
17. Process according to any of claims 14 to 16 characterised in that the direct heat exchange of the scrubbed and prepared top gas with the sponge iron particles is effected in a cooling assembly into which the hot sponge iron particles being carried out of the direct reduction assembly are transported via a downpipe.
18. Process according to claim 17, characterised in that the separation of the sponge iron particles into fine grain and coarse grain fractions is effected after the direct heat exchange with the prepared top gas.
19. Process according to claim 1 to 18, characterised in that the sponge iron particles of the coarse grain fraction are cooled by cooled, cleaned and prepared top gas from the direct reduction assembly.
20. Process according to claims 1 to 19, characterised in that a part of the top gas of the direct reduction assembly is fed after scrubbing and cooling in a top gas scrubber to the melt-down gasifier as an oxygen carrier or gasifying agent.
21. Process according to claim 20, characterised in that a fluidized layer is formed in the melt-down gasifier and the top gas blown into it.
22. Process according to any of claims 1 to 21, characterised in that the reduction gas produced in the melt-down gasifier is freed of dust in at last one cyclone before it is fed to the direct reduction assembly and at least a part of the solid particles separated in the cyclone and removed therefrom is fed back into the melt-down gasifier.
23. Process according to claim 21 to 22, characterised in that the cyclone extract is blown together with the top gas as a feed gas into the melt-down gasifier.
24. Process according to claim 23, characterised in that the cyclone extract is blown, with the top gas after mixing with oxygen or air, into the melt-down gasifier via at least one burner.
25. Plant for carrying out the process of any of claims 1 to 24, having a direct reduction assembly arranged above a melt-down gasifier, which has at its lower end an extractor device for hot sponge iron, of which the outlet opening is connected to the melt-down gasifier through at least one connector duct, characterised in that a coarse grain separator (7) is inserted into the connector duct between the direct reduction assembly (2) and the melt-down gasifier (1), of which separator the outlet opening (8) for the fine grain fraction is connected with the melt-down gasifier (1) and the outlet opening (11) for the coarse grain fraction with a special melt-down assembly or with a device (13) for heat compacting it, rendering it inert or cooling it.
26. A plant according to claim 25, characterised in that the coarse grain separator (7) is provided in the form of an inclined drop channel (38) with at least one nozzle (39) branching off downwardly from it, in which the fine particles are removed downwardly at the conveyance of the bulk material and are extractable in measured amounts via the nozzle (39), while the coarse particles are conveyed further on.
27. A plant according to claim 25, characterised in that the coarse grain separator (7) includes a thermally resistant sieve or a grill.
28. A plant according to claim 27, characterised in that the sieve or grill can be set in oscillation by a vibrator.
29. A plant according to any of claims 25 to 28, characterised in that the outlet opening (8) of the coarse grain separator (7) for the fine grain fraction is connected via at least one pipe (9) with a container (10), which includes an extractor device which is connected by at least one down pipe (17) with the melt-down gasifier.
30. A plant according to claim 29, characterised in that the pipe (17) projects from above into the interior of the melt-down gasifier (1) as far as the neighbourhood of the upper boundary of the fluidized bed of coal formed in the melt-down gasifier, and cascade-form projections (35) and/or a baffle plate (36) at the lower end of the pipe and provided.
31. A plant according to claim 30, characterised in that the baffle plate (36) is in the form of a truncated cone.
32. A plant for carrying out the process according to any of claims 1 to 24, having a direct reduction shaft furnace (2) which at the top has an inlet device (3) for the particulate iron ore and a gas outlet (5) for the used reduction gas (top gas) and, below, has an extractor device (41) for the sponge iron particles produced by direct reduction from the iron ore, and also a gas inlet (4) for hot reduction gas, a melt-down gasifier (1), which has, in its upper region, openings (17, 15, 45) for admitting sponge iron particles, coal and additives as well as a gas outlet (43) for produced reduction gas (raw gas) and in its lower region outlets (21, 22) for liquid pig iron and liquid slag, and, above the slag level, at least one nozzle or burner (23, 23a) for blowing in gas and fine grain solids to form a gasifying zone, a cooling assembly (13a) for hot sponge iron particles, which includes an inlet opening (46) at the top for the hot sponge iron particles and an outlet (48) for the cooling gas and, below, an outlet opening (14) for the cooled sponge iron particles and also an inlet (49) for the cooling gas, also having a top gas scrubber (28) connected with the top gas outlet (5) of the direct reduction shaft furnace (2), and also having pipes connecting the individual assemblies, with valves and compressors, characterised in that a classifying device (7a) is provided for separating the sponge iron particles, having an outlet opening (8) for a fine grain fraction, which is connected by a pipe (9) to an upper opening (17) of the melt-down gasifier (1), and an outlet opening (11) for a coarse grain fraction.
33. A plant for carrying out the process according to claim 32, characterised in that the gas outlet (51) of the top gas scrubber (28) is connected to the nozzle (23a) in the lower section of the melt-down gasifier (1).
34. A plant according to claim 32 or 33, characterised in that the inlet opening (46) of the cooling assembly (13a) is connected by a down pipe (6) to the extractor device (41) of the direct reduction shaft furnace (2) and the outlet opening (14) of the cooling assembly (13a) is connected to the classifying device (7a).
35. A plant according to any of claims 32 to 34, characterised in that the gas outlet (51) of the top gas scrubber (28) is connected to a C02 separator (2a) and the cooling gas inlet (49) of the cooling assembly (13a) is connected with the gas outlet (54) of the C02 separator (29) and the cooling gas outlet (48) of the cooling assembly is connected with an inlet nozzle (44) in the head (42) or in the exhaust duct (61) of the melt-down gasifier (1).
36. A plant according to any of claims 32 to 35, characterised in that the gas outlet (43) for the reduction gas produced in the melt-down gasifier (1) is connected to at least one cyclone (62) and the outlet opening (64) for the precipitated solids of the cyclone is connected to the pipe duct (16) from the top gas scrubber (28) to the lower inlet nozzle (23a) of the melt-down gasifier (1).
EP83111296A 1982-11-15 1983-11-11 Process and device for the instant production of reduced iron pellets and liquid iron from iron oxide pellets Expired EP0111176B1 (en)

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AT83111296T ATE19658T1 (en) 1982-11-15 1983-11-11 PROCESS AND PLANT FOR THE DIRECT PRODUCTION OF SPONGE IRON PARTICLES AND LIQUID PIG IRON FROM CHILLED IRON ORE.

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DE3242232 1982-11-15
DE3242232 1982-11-15
DE19833328373 DE3328373A1 (en) 1982-11-15 1983-08-05 METHOD AND SYSTEM FOR THE DIRECT PRODUCTION OF SPONGE IRON PARTICLES AND LIQUID PIPE IRON FROM PIECE IRON ORE
DE3328373 1983-08-05

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT394201B (en) * 1989-02-16 1992-02-25 Voest Alpine Ind Anlagen METHOD FOR GENERATING COMBUSTIBLE GASES IN A MELT-UP CARBURETTOR
US6258148B1 (en) 1996-07-11 2001-07-10 Voest-Alpine Industrieanlagenbau Gmbh Method of charging metal carriers to a melt-down gasifying zone

Families Citing this family (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3438487A1 (en) * 1984-10-17 1986-04-24 Korf Engineering GmbH, 4000 Düsseldorf METHOD FOR THE PRODUCTION OF RAW IRON
AT381116B (en) * 1984-11-15 1986-08-25 Voest Alpine Ag METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND DEVICE FOR IMPLEMENTING THE METHOD
SU1479006A3 (en) * 1984-11-26 1989-05-07 Фоест-Альпине (Фирма) Method of producing molten iron or steel products and reducing gas in melting gasifier
DE3503493A1 (en) * 1985-01-31 1986-08-14 Korf Engineering GmbH, 4000 Düsseldorf METHOD FOR THE PRODUCTION OF RAW IRON
DE3504346C2 (en) * 1985-02-06 1986-11-27 Korf Engineering GmbH, 4000 Düsseldorf Method and device for the production of sponge iron particles and liquid pig iron
US4685964A (en) * 1985-10-03 1987-08-11 Midrex International B.V. Rotterdam Method and apparatus for producing molten iron using coal
DE3603894A1 (en) * 1986-02-05 1987-08-06 Korf Engineering Gmbh METHOD FOR PRODUCING LIQUID PIPE IRON OR STEEL PRE-MATERIAL
US4913734A (en) * 1987-02-16 1990-04-03 Moskovsky Institut Stali I Splavov Method for preparing ferrocarbon intermediate product for use in steel manufacture and furnace for realization thereof
AU596758B2 (en) * 1987-11-13 1990-05-10 Jp Steel Plantech Co. Metal-making apparatus involving the smelting reduction of metallic oxides
US4981628A (en) * 1988-10-11 1991-01-01 Sudamet, Ltd. Repairing refractory linings of vessels used to smelt or refine copper or nickel
AT390622B (en) * 1988-10-25 1990-06-11 Voest Alpine Ind Anlagen METHOD AND INSTALLATION FOR THE PRODUCTION OF LIQUID PIG IRON
DE4037977A1 (en) * 1990-11-29 1992-06-11 Voest Alpine Ind Anlagen METHOD FOR THE PRODUCTION OF RAW IRON OR IRON SPONGE
US5354356A (en) * 1992-10-06 1994-10-11 Bechtel Group Inc. Method of providing fuel for an iron making process
US5320676A (en) * 1992-10-06 1994-06-14 Bechtel Group, Inc. Low slag iron making process with injecting coolant
US6197088B1 (en) 1992-10-06 2001-03-06 Bechtel Group, Inc. Producing liquid iron having a low sulfur content
US5397376A (en) * 1992-10-06 1995-03-14 Bechtel Group, Inc. Method of providing fuel for an iron making process
AT402506B (en) * 1993-01-26 1997-06-25 Holderbank Financ Glarus METHOD FOR THE PRODUCTION OF RAW IRON AND CEMENT CLINKER
US5958107A (en) * 1993-12-15 1999-09-28 Bechtel Croup, Inc. Shift conversion for the preparation of reducing gas
AT406483B (en) 1995-07-19 2000-05-25 Voest Alpine Ind Anlagen METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD
AT406482B (en) * 1995-07-19 2000-05-25 Voest Alpine Ind Anlagen METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD
AT406480B8 (en) * 1995-07-19 2000-07-25 Voest Alpine Ind Anlagen METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD
AT403381B (en) 1996-06-10 1998-01-26 Voest Alpine Ind Anlagen METHOD AND SYSTEM FOR CHARGING METAL CARRIERS IN A MELTING GASIFICATION ZONE
AT403696B (en) * 1996-06-20 1998-04-27 Voest Alpine Ind Anlagen MELTING CARBURETTOR AND SYSTEM FOR THE PRODUCTION OF A METAL MELT
AT404022B (en) 1996-11-08 1998-07-27 Voest Alpine Ind Anlagen METHOD AND INSTALLATION FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS FROM IRON-CONTAINING MATERIAL
AT404362B (en) 1996-12-17 1998-11-25 Voest Alpine Ind Anlagen METHOD AND MELTING CARBURETOR FOR PRODUCING LIQUID METAL
AT510586B1 (en) * 2011-05-12 2012-05-15 Siemens Vai Metals Tech Gmbh METHOD AND DEVICE FOR DISPERSING DUST PARTICLES FROM A DUST LINE
CN113913579B (en) * 2021-10-12 2023-01-24 中冶赛迪工程技术股份有限公司 Circulation method for cooling hot sponge iron

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1353716A (en) * 1916-10-05 1920-09-21 Charles S Bradley Production of iron and steel
US2747988A (en) * 1951-04-23 1956-05-29 Kenneth R Marsden Method for the recovery of pure iron oxide and iron from oxidic iron ores
BE642457A (en) * 1963-12-23
US3199974A (en) * 1964-05-25 1965-08-10 Hydrocarbon Research Inc Fluidized iron ore reduction process for production of iron powder
DE2401540B2 (en) * 1974-01-14 1975-11-13 Fried. Krupp Gmbh, 4300 Essen Method for melting sponge iron
DE2401909C3 (en) * 1974-01-16 1985-06-27 Fried. Krupp Gmbh, 4300 Essen Process for the production of steel
US4094665A (en) * 1977-05-13 1978-06-13 Stora Kopparbergs Bergslags Ab Method for simultaneous combined production of electrical energy and crude iron
DE2905339A1 (en) * 1979-02-13 1980-08-21 Metallgesellschaft Ag METHOD FOR PRODUCING STEEL
US4316739A (en) * 1979-07-16 1982-02-23 Midrex Corporation Method for producing molten iron
US4248626A (en) * 1979-07-16 1981-02-03 Midrex Corporation Method for producing molten iron from iron oxide with coal and oxygen
US4304597A (en) * 1980-03-20 1981-12-08 The Direct Reduction Corporation System for control of sinter formation in iron oxide reducing kilns
CA1125505A (en) * 1980-05-09 1982-06-15 William E. Creswick Fabricated tuyere
US4436551A (en) * 1981-10-26 1984-03-13 Sumitomo Heavy Industries, Ltd. Process for making steel from direct-reduced iron
US4412858A (en) * 1982-07-12 1983-11-01 Hylsa, S.A. Method of converting iron ore into molten iron

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT394201B (en) * 1989-02-16 1992-02-25 Voest Alpine Ind Anlagen METHOD FOR GENERATING COMBUSTIBLE GASES IN A MELT-UP CARBURETTOR
US6258148B1 (en) 1996-07-11 2001-07-10 Voest-Alpine Industrieanlagenbau Gmbh Method of charging metal carriers to a melt-down gasifying zone
US6491864B2 (en) 1996-07-11 2002-12-10 Voest-Alpine Industrieanlagenbau Gmbh Plant for charging metal carriers to melt-down gasifying zone

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PL142647B1 (en) 1987-11-30
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ATE19658T1 (en) 1986-05-15
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PH20286A (en) 1986-11-18
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SU1313354A3 (en) 1987-05-23
ES527233A0 (en) 1984-08-01
US4543123A (en) 1985-09-24
DE3363431D1 (en) 1986-06-12
DD210310A5 (en) 1984-06-06
DE3328373A1 (en) 1984-05-17
AU569481B2 (en) 1988-02-04
US4542889A (en) 1985-09-24

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